Counterflow adsorption filter column for water treatment

ABSTRACT

The present invention relates to a method for treatment and/or purification of water, in particular wastewater or drinking water, preferably for the adsorptive removal of inorganically or organically-based, impurities, such as trace substances and/or micropollutants, wherein, in a counterflow filter device, e.g. a counterflow adsorption filter column, the water that is to be treated and/or that is to be purified firstly, and, secondly, an, in particular particulate, adsorption material are conducted in a counterflow direction. In particular, a procedure is followed in such a manner that the water to be treated and/or purified is passed through a bed of the adsorption material present in the counterflow filter device for the adsorptive removal of impurities and the bed is exchanged and regenerated by preferably continuous removal and supply of the adsorption material in counterflow to the water that is to be treated and/or that is to be purified.

CROSS-REFERENCES TO RELATED APPLICATIONS

This patent application is a continuation of U.S. application Ser. No.14/777,178, entitled “COUNTERFLOW ADSORPTION FILTER COLUMN FOR WATERTREATMENT” filed on Sep. 15, 2015, which claims priority to PCT/EP2014/053289, filed Feb. 20, 2014, and to German Applications DE 10 2013004 407.3 filed Mar. 15, 2013; DE 10 2013 004 747.1 filed Mar. 20, 2013;and DE 10 2013 006 711.1 filed Apr. 19, 2013, and incorporates all byreference herein, as if each one were independently incorporated in itsentirety.

BACKGROUND OF THE INVENTION

The present invention relates to the technical field of the treatment ofwater, especially of wastewater or drinking water. More particularly,the present invention relates to the technical field of the treatment orpurification of water in the drinking water or wastewater sector.

More particularly, the present invention relates to a method fortreatment or purification of water (untreated water), especially ofwastewater or drinking water, preferably for adsorptive removal ofinorganic- or organic-based, especially organic-based, contaminants suchas trace substances and/or micropollutants.

The present invention further relates to a purification plant,preferably for treatment or purification of water, especially ofwastewater or drinking water.

The present invention additionally relates to a countercurrent filterapparatus, especially countercurrent adsorption filter column, which isequally suitable for treatment and purification of water, especially ofwastewater or drinking water, and preferably for removal, especiallyadsorptive removal, of inorganic- or organic-based, especiallyorganic-based, contaminants.

The present invention finally relates to the uses of the purificationplant of the invention and of the countercurrent filter apparatusaccording to the invention, and also of specific adsorption materials inthe method according to the invention for treatment or purification ofwater, especially wastewater or drinking water.

Increasing pollution of the aquatic environment, for example of surfacewater bodies, but also of groundwater and drinking water, constitutes amajor environment-specific problem, especially since water in the formof drinking water is one of the most important and irreplaceable meansof sustaining life. More particularly, the introduction of wastewatercontaminated with contaminants into water systems and the deployment ofcontaminated sewage sludge or the like, for example on agriculturalland, lead to corresponding contamination and pollution both of surfacewater and of groundwater.

A particular problem in this context is that of microcontaminants, forwhich another synonymous term is trace substances or micropollutants.These include not only industrial chemicals and flame retardants butespecially also active pharmaceutical ingredients and humanpharmaceuticals, such as analgesics, active hormone ingredients or thelike, which are secreted in unchanged form or as conjugates ormetabolites after chemical conversion in the human organism and, as aresult, get into communal wastewater, for example. A further problem isthat particular industrial chemicals such as plasticizers, especiallybisphenol A, x-ray contrast agents such as amidotrizoic acid andiopamidol, surfactants, such as perfluorinated surfactants, pesticidesand the like, since substances of this kind, even in small amounts, havea high toxic potential and/or low biocompatibility. Further examples ofmicrocontaminants generally include antiknock agents such as methyltert-butyl ether (MTBE).

In addition, what are called dissolved organic compounds or dissolvedorganic carbons (DOCs) may be cited, which may likewise be present ascontaminants in water.

The aforementioned substances or substance classes especially have thefeature in common that, even in the event of uptake of very smallamounts in the μg or even in the ng range, they can have a considerableinfluence on the human organism, for example in terms of a hormonaleffect, the endocrine disruptor character thereof, the development ofresistances or the like.

Human pharmaceuticals, particularly because of the demographictransformation and rising individual life expectancy, with theassociated increased consumption of medicaments, will get into theenvironment via communal wastewater pathways in an even greater amountand number in the future, which is similarly true of veterinarypharmaceuticals because of the general rise in meat consumption with theassociated forms of animal keeping.

In addition, pharmacologically active substances which are used inveterinary medicine can similarly get into surface water bodies and intothe groundwater, especially as a result of deployment of correspondinglycontaminated slurry and subsequent leaching of the agricultural landfertilized thereby by precipitation, such that the correspondingmicrocontaminants can be flushed into water systems or into thegroundwater.

Because of the toxicity, persistence and high bioaccumulation potentialof microcontaminants or trace substances and the increasing use of suchsubstances, there is a great need to minimize the introduction orrelease of microcontaminants into surface water bodies and into thegroundwater, and a primary aim in this context should be considered thatof effectively treating contaminated wastewater from domestichouseholds, from industry and from medical facilities such as hospitalsor other healthcare facilities in order to reduce the level of thecorresponding microcontaminants. In this context, the purification ofalready contaminated drinking water, especially in the waterworks beforefeeding into the drinking water grid, is also of high relevance,especially since the microcontaminants in question, because of theirincreasing presence in the aquatic environment, are increasingly presentor detectable in drinking water, sometimes in critical amounts.

This is because there may otherwise be unwanted release of theaforementioned substances through the sewage treatment plant effluentinto surface water bodies and subsequently also into the groundwater,especially if the microcontaminants are not adequately removed from theoriginal wastewater. Similarly, contaminated wastewater can otherwiseget to the end user, which is similarly undesirable.

It can thus be stated in summary that trace substances ormicrocontaminants, especially in the form of medicaments, but also ofindustrial and industrial/mechanical origin, are present in wastewaterto an increasing degree and can often also get into surface water bodiesand into the groundwater as a result of often inadequate treatment orpurification of the wastewater, which in turn results in an increasedrisk of contamination of drinking water, associated with a highendangerment potential for man and the environment.

Against this background, numerous approaches have been pursued in theprior art, which are intended to provide a basis for freeingcontaminated water, especially contaminated wastewater or drinkingwater, of microcontaminants or trace materials, for which purpose plantsusing various filter apparatuses for wastewater treatment in sewagetreatment plants on the one hand and for drinking water treatment on theother hand have been designed, particularly in waterworks. However, theknown approaches for water purification do not always lead to thedesired success.

Thus, one technical approach for reduction of microcontaminant or tracesubstance levels involves chemical breakdown of the microcontaminantspresent in untreated water by means of oxidation processes, theunderlying methods generally being referred to as advanced oxidationprocesses (AOP). These include, for example, an ozone and/or UVtreatment of the water to be treated. A disadvantage in the case ofthese methods, however, is the high energy costs that they ofteninvolve, the complex removal of residual ozone in the treated water andthe unwanted formation of toxic metabolites or degradation products ofthe microcontaminants in question.

A further approach to purification of water in the prior art involvesusing membrane-based filter plants, in which case, for example, theprinciple of reverse osmosis (RO) and of nanofiltration (NF) andultrafiltration (UF) is used. However, purifying concepts of this kindare associated with the disadvantage that sometimes complex and costlyand also maintenance-intensive filter plants have to be designed andoperated, the operation of the corresponding plants being accompanied byhigh energy costs in some cases. In addition, highly contaminated toxicresidues often arise, the disposal of which constitutes a furtherlogistical challenge. Other disadvantages are the sometimes lowselectivity and the short operating times and/or service lives of thecorresponding filter plants, it being possible for operation to bedisrupted for a prolonged period, for example, by (micro-)biologicalgrowth on the membranes.

In addition, a further method for reducing the content ofmicrocontaminants in water involves removing the microcontaminants fromthe water by means of conventional activated carbons. The correspondingconcepts together with the technical implementation and the conventionalactivated carbons used for the purpose, however, are oftendisadvantageous in that the filter design in the prior art results inlow filter capacities and similarly short operating times and/or servicelives. Another problem is sometimes (micro-)biological growth in thefilter units as such or on the activated carbons used, since this canlead to a reduction in the filter throughput or to a reduction inadsorption capacity.

Moreover, the conventional activated carbons used in the prior art oftendo not have adequate selectivity and have only low mechanical stability,which can lead to premature abrasion, especially with disadvantageousdust or sludge formation.

More particularly, the prior art often provides for the use of granularadsorptions, but these have a high proportion of binder, and of powderedcharcoal, the charcoals used here being based, for example, on hard coalor on charcoals having coconut shells or pitch as starting material.Activated carbons of this kind are often neither mechanically stable norsatisfactory in terms of their adsorption properties, since they oftenhave only a low adsorption capacity and selectivity. A furtherdisadvantage of such activated carbons is that the correspondingindustrial filter plants can become blocked as a result of sludgeformation, for example on the basis of powdered charcoal or charcoalabrasion, which reduces the throughput capacity and hence the operatingtime and/or service life.

Moreover, the concepts realized in the prior art involving regenerationof spent activated carbon, i.e. that contaminated with contaminants, isoften impossible or can be accomplished only with a high level of costand inconvenience, especially using steam in a high-temperature process,accompanied by high energy costs and a loss of adsorptions, especiallyas a result of unwanted burnoff.

The industrial units and plants envisaged for the use of activatedcarbon are additionally often complex in terms of construction and leadto reduced efficiency in the overall filter assessment. Thus, theactivated carbon adsorption stages known in the prior art, which areconnected downstream of a mechanical treatment stage and a biological orchemical treatment stage, for example in the context of wastewatertreatment, consist of a reaction tank on the one hand and a downstreamsedimentation tank on the other hand, the activated carbon being added,especially in pulverulent form, to the reaction tank, and the activatedcarbon laden with contaminants being removed in the sedimentation tank,often using precipitants or flocculants. Regeneration of the spentcharcoal component thus obtained is often impossible, and so the spentactivated carbon has to be utilized thermally together with the sewagesludge. The merely thermal final utilization of spent activated carbonalso worsens the carbon footprint and hence the overall environmentalassessment of the underlying methods.

Plants of this kind for purification of water using conventionalactivated carbon additionally entail a high space demand, since thecorresponding adsorption tanks are designed as open long-life filterswhich can have a length of more than 10 m. An additional factor is theuse of large amounts of activated carbon, since the activated carbonsused should be used the long-life filters in a bed having a height of 2to 3 m, and so a total volume of 200 m³ to 300 m³ of activated carbonper tank is required.

A further approach to adsorptive treatment of water in the prior artinvolves using closed filter systems having activated carbon in the formof a bed or in a fixed bed. Systems of this kind can also be used, forexample, as a downstream purification stage in the context of thetreatment of drinking water. As stated above, however, these are filtersystems having a closed design in relation to the adsorption material,such that no exchange of the activated carbon component is possibleduring the operation of the underlying filter plants. In this context,the prior art especially envisages percolation of the water to bepurified, especially through a fixed bed filter or a bed of activatedcarbon based on closed pressure filters. A particular disadvantage hereis that systems of this kind are exhausted quickly in terms of thesubstances to be adsorbed and hence only a limited filter capacity ispresent. Moreover, it is necessary to renew the entire adsorptionmaterial in the filter apparatus after the adsorption material hasbecome exhausted, which results in shutdown of the filter element inquestion. To compensate for this, complex bypass connections or the useof parallel filter components is required, which makes plants of thiskind complex in terms of construction and costly. Another particulardisadvantage in this context is the high space demand of such plants.

The closed filter systems envisaged in the prior art, especiallypressure filters, are additionally designed such that they have atubular construction with a generally high diameter and great height,especially since, because of the closed filter arrangement, similarlylarge volumes of activated carbon are required in the filter system.Pressure filter systems of this kind often have a ratio of height todiameter in the range from about 2 to 3 or less, such that systems ofthis kind, for this reason too, have a high space demand and sometimesnonoptimal flow conditions within the filter.

Moreover, in the case of such filter concepts, only a limited height ofthe bed is possible, since, for technical reasons, significant headspaceis required within the filter apparatus. More particularly, the closedfilter systems of the prior art cited above have only a low height ofthe adsorption component within the filter and hence only a lowadsorption height, the overall result of which is nonoptimalexploitation of the total filter volume. In this context, the prior artpressure filter systems described have a ratio of total column height orfilter height to the height of the adsorption material in the filter of5 to 10 or more.

Moreover, it is a requirement in the aforementioned plants or systemsfor the water to be purified to be free of suspended materials to a highdegree, in order to prevent premature blockage of the filter system. Inthis regard, another disadvantage in relation to the prior art is thatreprocessing or recycling of spent activated carbon is possible only toa very limited degree, one to two recycling runs at best being possible,the effect of which is likewise that large amounts of adsorptions usedhave to be replaced by new material. More particularly, this is alsoassociated in the prior art with a high loss of activated carbon, whichmay be up to 25% of the original charge used, the losses in questionbeing caused particularly by dust losses and burnoff. More particularly,efficient reactivation is often impossible.

The above-cited methods and plants using activated carbon as adsorptionmaterial allow batchwise exchange of the activated carbon at best, whichleads to disadvantageous interruptions of operation and a reduction inefficiency.

Moreover, the aforementioned prior art systems are often inefficient inthat satisfactory purification of water to be treated cannot beachieved, especially with regard to problem materials such as dissolvedorganic carbons (DOCs), perfluorinated surfactants such asperfluorooctanesulfonate (PFOS), antiknock agents such as methyltert-butyl ether (MTBE), x-ray contrast agents such as iopamidol andamidotrizoic acid.

Furthermore, in relation to the prior art for the plants describedtherein, there are also unfavorable circulation factors, which representthe ratio of spent activated carbon and that being regenerated to theactivated carbon present in the filter system and hence in use for thepurposes of purification. In this context, in the prior art, the bestconversion factors possible are of 100 or more, especially 200 to 300 ormore.

Moreover, such prior art filter systems have relatively low superficialvelocities or filtering rates of only 10 m/h at most, particularly inorder to enable a certain purification efficiency at all in this way.However, this results in low volumes or amounts of purified water.

Because of the sometimes nonoptimal filter properties of the prior artsystems, especially with regard to the closed pressure filters citedabove, the result is generally relatively low specific water throughputsbefore the breakthrough of a trace substance. For example, in the caseof prior art systems, the specific water throughput before thebreakthrough of the trace substances amidotrizoic acid, given a startingconcentration of 290 ng/L in the water for treatment, is about 25 m³/kgof activated carbon.

DE 1 642 396 A1 relates to a method for treatment of wastewater, whereinsuspended solids are first removed and wherein the sieved untreatedwater is treated with a flocculant and the supernatant water isseparated from the flocculated material formed and passed throughactivated carbon beds. The activated carbon beds are back-flushed andregenerated periodically. According to this design, there is thus merelydiscontinuous or batchwise regeneration of the activated carbon, butthis is unfavorable or disadvantageous from a process technology pointof view, since the operating times are reduced or the installation ofseveral parallel filter components is necessary as a result. Moreover,the back-flushing in particular is associated with sometimes high lossesof adsorption material.

Moreover, DE 2 040 061 A1 relates to a plant for disinfection ofwastewater, using disinfectants specific to this purpose. Reduction ofmicrocontaminant levels is not possible on the basis of this design, andthe use of disinfectants, moreover, is problematic from an environmentalpoint of view. More particularly, batchwise operation of the plant withback-flushing of the filter element is envisaged, the intention being toremove what is called a return sludge from the apparatus in this way.

Furthermore, German utility model specification DE 88 15 345 U1 relatesto a water treatment system, especially for treatment or provision ofpollutant-free drinking water, wherein the water treatment system isequipped with a plate module which works by the principle of reverseosmosis. This design is disadvantageous in that the system is ofcomparatively low selectivity and has to be operated with high energyinput, giving contaminated toxic residues.

Moreover, DE 10 2008 041 164 A1 relates to a method for treating waterfor removal of halide ions by oxidative halogenation of an organiccompound added to the water, which is subsequently removed, withconversion of chlorate, iodate and bromate ions remaining in the waterto the corresponding halide ions, which is to be followed by anotheroxidative halogenation. A method of this kind is complex in terms of theprocess and additionally inefficient in relation to a multitude ofmicrocontaminants.

Finally, EP 1 044 982 A1 relates to a water treatment method whichcomprises the addition of ozone to untreated water and the filtering ofthe untreated water using an ozone-resistant membrane, with the optionof further treatment of the filtrate with activated carbon or a reverseosmosis membrane. This purification, which is complex in terms ofprocess technology, is sometimes costly and has not been optimized forcontinuous operation, especially with regard to the use of the activatedcarbon.

SUMMARY

Against this technical background, it is therefore an object of thepresent invention to provide an efficient method and correspondingplants or apparatuses for treatment or purification of water, such aswastewater or drinking water, wherein the above-outlined disadvantagesof the prior art are to be at least substantially avoided or else atleast mitigated.

More particularly, it is an object of the present invention to providean efficient method and plants or apparatuses for this purpose, whereinparticularly inorganic- or organic-based, especially organic-based,contaminants such as trace substances or microcontaminants are to beremoved from the water for treatment or purification.

In this context—in a further object of the present invention—moreparticularly, an efficient system or an efficient plant havingappropriate apparatuses, especially for performance of the method of theinvention, is to be provided, the intention being to ensure higheconomic viability overall with simultaneously high purificationefficiency, especially with regard to the operating time, theconsumption of adsorptions for purification of the water to be treatedand the energy input required. At the same time, continuous oruninterrupted operation of the plant or system and/or continuous oruninterrupted performance of the method is preferably to be ensured.

More particularly, it is a further object of the invention again toprovide a corresponding system or purification plant, especially forperformance of the method of the invention, by means of which theadsorbent for processing of the water to be treated can be used in anefficient and lasting manner, especially with regard to prolonged anduninterrupted operating times and service lives of the filterapparatuses used in this connection.

Moreover, in a further objective of the present invention, correspondingpurification plants and apparatuses are to be provided, which shall alsobe optimized overall in terms of space and hence be space-saving overalland which shall have a high economic compatibility and an excellentecological assessment overall.

The objective outlined above is achieved in accordance with theinvention by the subject matter of method claims, which relates to themethod of the invention for treatment or purification of water,especially of wastewater or drinking water, preferably for adsorptiveremoval of inorganic- or organic-based, especially organic-based,contaminants such as trace materials or microcontaminants; furtheradvantageous developments and configurations of this aspect of theinvention are the subject of the corresponding further independentmethod claims and dependent method claims.

The present invention further provides the purification plant of theinvention, preferably for treatment or purification of water, as definedin the corresponding independent claims; further advantageousdevelopments and configurations of the purification plant of theinvention are the subject of the corresponding dependent claims.

The present invention additionally provides a countercurrent filterapparatus, especially countercurrent adsorption filter column,preferably for treatment or purification of water, as defined in thecorresponding independent apparatus claim; further advantageousdevelopments and configurations of the countercurrent filter apparatusof the invention are the subject of the respective dependent apparatusclaims.

Finally, the present invention in turn further provides for the use ofthe purification plant of the invention or of the adsorption materialused in the context of present invention, and of the countercurrentfilter apparatus of the invention in the method of the invention fortreatment or purification of water according to the description herein.

It will be appreciated that configurations, embodiments, advantages andthe like that are cited hereinafter for just one aspect of the inventionfor the purpose of avoiding repetition do of course also applycorrespondingly in relation to the other aspects of the invention.

Furthermore, it will be appreciated that, in the case of values, numbersand ranges stated hereinafter, the ranges stated should not beunderstood in a restrictive manner;

it will be apparent to the person skilled in the art that, depending onthe individual case or based on the application, it is possible todeviate from the stated ranges and figures, without leaving the scope ofthe present invention.

Moreover, all the values and parameters stated hereinafter, or the like,can be determined or ascertained in principle by standardized orexpressly specified determination methods, or else by determinationmethods familiar per se to those skilled in the art.

With these provisions, the present invention is described in detailhereinafter.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 provides a schematic diagram or overview of the purificationplant A of the invention, preferably for treatment or purification ofwater or untreated water AW, preferably for adsorptive removal ofinorganic- or organic-based, especially organic-based, contaminants suchas trace materials and/or micropollutants, in one embodiment of theinvention;

FIG. 2 provides a schematic section diagram of the countercurrent filterapparatus 1 of the invention, especially countercurrent adsorptionfilter column, in a preferred embodiment of the invention, wherein thecountercurrent filter apparatus 1 has at least one housing 2, saidhousing 2 having at least one adsorption and/or countercurrent zone 3and at least one water entry region 4 and at least one water exit region5, and wherein the water entry region 4 has at least one adsorptionmaterial outlet 6 and wherein the water exit region 5 has at least oneadsorption material inlet 7;

FIG. 3 provides a further schematic section diagram of thecountercurrent filter apparatus 1 of the invention, especiallycountercurrent adsorption filter column, in a preferred embodiment ofthe invention and with an illustration of the flow or transport of thewater W on the one hand and the adsorption material AK on the other handthat is present in the countercurrent filter apparatus 1, so of the bed15, especially the loose bed 15, of the adsorption material present inthe countercurrent filter apparatus.

DETAILED DESCRIPTION OF THE INVENTION

The present invention thus provides—in a first aspect of the presentinvention—a method for treatment and/or purification of water,especially of wastewater or drinking water, preferably for adsorptiveremoval of inorganic- or organic-based, especially organic-based,contaminants such as trace substances and/or micropollutants. It is afeature of the method of the invention that, in a countercurrent filterapparatus, especially countercurrent adsorption filter column, the waterto be treated and/or purified on the one hand and an adsorptionmaterial, especially a particulate adsorption material, on the otherhand are conducted in countercurrent and/or in opposite directions toone another, especially in such a way that the water to be treatedand/or purified is passed through a bed of the adsorption materialpresent in the countercurrent filter apparatus for adsorptive removal ofcontaminants and the bed is exchanged and regenerated by preferablycontinuous removal and supply of the adsorption material incountercurrent to the water to be treated.

In the context of the present invention, in a particularly preferredembodiment of the invention, it may be the case that the adsorptionmaterial is conducted and/or introduced, especially continuously, intothe countercurrent filter apparatus. In addition, in this context, theadsorption material may especially be conducted continuously out ofand/or removed continuously from the countercurrent filter apparatus.

In a further, particularly preferred embodiment of the invention, it mayadditionally be the case that the adsorption material which has beenconducted out of and/or removed from the countercurrent filter apparatusand/or laden with the contaminants, is sent to and/or subjected to aregeneration and/or recycling operation, especially a continuous and/orespecially a thermal regeneration and/or recycling operation. In thisway, it is especially possible to remove or desorb the contaminantswhich have been taken up or adsorbed by the activated carbon beforehand,so as to result in a regenerated or unused or unladen or freshadsorption material. More particularly, the regenerated or unused orunladen or fresh adsorption material may be conducted and/or introduced,especially continuously, back into the countercurrent filter column.

The wording “conduct in countercurrent and/or in opposite directions toone another”, as used in the context of present invention, shouldespecially be understood so as to mean that, in relation to the water tobe treated or purified on the one hand and the adsorption material onthe other hand, there is a respective mass transfer or mass flow in themanner of a countercurrent principle, i.e. in opposite directions of therespective mass transfers or mass flows relative to one another; moreparticularly, the water to be treated or purified on the one hand andthe adsorption material on the other hand are in direct contact with oneanother in the countercurrent filter apparatus or in the adsorption orcountercurrent zone (which can also be referred to synonymously as masstransfer zone) of the countercurrent filter apparatus, and so, as aresult, substances present in the water can be taken up or adsorbed bythe adsorption material, said substances especially being thecontaminants present in the water to be treated or purified, such astrace substances or microcontaminants.

The water to be treated or purified on the one hand and the adsorptionmaterial on the other hand thus flow in opposite directions to oneanother according to the inventive design, with into the respective(main) flow directions opposed to one another at least essentially by180°.

More particularly, in general, the water to be treated or purified, inthe operating state or use state of the countercurrent filter plant,flows from the water entry region through the adsorption orcountercurrent zone to the or into the water exit region of thecountercurrent filter plant, whereas the adsorption material flows or istransported from the water exit region through the adsorption orcountercurrent zone to the or into the water entry region of thecountercurrent filter plant.

In this context—in a preferred embodiment of the invention, according towhich the countercurrent filter apparatus used in the method of theinvention, based on the longitudinal axis thereof, is operated invertical arrangement or positioning—the water is introduced into a lowerend or into a water entry region disposed at the lower end of thecountercurrent filter apparatus, while the adsorption material isintroduced into an upper end of the countercurrent filter apparatus,which simultaneously defines a water exit region. Within thecountercurrent filter apparatus, the result, in this embodiment, inrelation to the water, is thus a flow direction from the bottom upwardso to speak, with removal of the purified water or the resultingfiltrate from the countercurrent filter apparatus at the upper end,while, in relation to the adsorption material, there is a flow directionfrom the top downward so to speak in the countercurrent filterapparatus, the adsorption material laden with the contaminants thenbeing removed from the countercurrent filter apparatus at the lower end.

In the context of the method of the invention, the procedure mayespecially be such that the water to be treated or purified istransported into the countercurrent filter apparatus under pressure, forexample by means of (compression) pump apparatuses, or that the water orfiltrate which has been purified or freed of the contaminants is removedfrom the countercurrent filter apparatus with application of a reducedpressure, for example using (suction) pump apparatuses. In addition, theadsorption material can be introduced into the countercurrent filterapparatus, for example by means of pressurization, and/or removed fromthe countercurrent filter apparatus by means of application of reducedpressure using appropriate pump apparatuses.

In this connection, in relation to the adsorption material, the pressureat the introduction site into the countercurrent filter apparatus shouldbe greater than the corresponding opposing pressure in thecountercurrent filter apparatus or in the adsorption and/orcountercurrent zone. Similarly, the pressure at the exit site of theadsorption material should be such that the pressure in thecountercurrent filter apparatus or in the adsorption and/orcountercurrent zone is greater than the pressure in the region thatfollows on from or is downstream of the exit site. For the feed of the(untreated) water to be treated or purified, it is correspondingly thecase that the feed pressure of the water is preferably greater than thepressure in the countercurrent filter apparatus or in the adsorptionand/or countercurrent zone, or that the pressure in the region thatfollows on from the countercurrent filter apparatus or the region of thewater drain arranged downstream thereof is lower than the correspondingpressure in the countercurrent filter apparatus or the adsorption and/orcountercurrent zone.

With regard to the transport of the adsorption material in thecountercurrent filter apparatus or in the adsorption and/orcountercurrent zone, the latter may firstly be caused and/or supportedby the corresponding pressurization or application of reduced pressure,especially as outlined above. It may likewise especially be the case inaccordance with the invention that the corresponding transport of theadsorption material within the countercurrent filter apparatus or in theadsorption and/or countercurrent zone is effected as a result of or byvirtue of support by gravity, i.e. to a certain degree by virtue of theheight of the bed itself, especially if the countercurrent filterapparatus is arranged vertically with respect to its longitudinal axis,accompanied by the mass transfer or mass flow of the adsorption materialfrom the top downward, so to speak.

The fundamental idea of the present invention is especially that themethod of the invention is conducted in a very specific countercurrentfilter apparatus as described in detail hereinafter, wherein, inrelation to the transport or flow of the water to be treated orpurified, the adsorption material used for purification of the water istransported in the opposite direction thereto or flows in the oppositedirection thereto, and so the water flow on the one hand and thetransport or flow of the adsorption material or the adsorption materialstream on the other hand are in countercurrent to one another in thecountercurrent filter apparatus. The water to be purified on the onehand and the adsorption material on the other hand are thus conducted orcontacted with one another in opposite transport or flow directions inthe countercurrent filter apparatus used in accordance with theinvention.

The adsorption material used in accordance with the invention, withinthe countercurrent filter apparatus, especially in the form of a loosebed or in the form of a moving bed and/or in the form of a (loose)moving bed, from which, especially on the feed side of the water to betreated or purified, spent adsorption material is especially withdrawnor drawn off continuously, and to which, on the exit site of thepurified water or filtrate, regenerated or unused adsorption material isadded again, so as to result in the above-described opposing transportprocess of the adsorption material in relation to the water to betreated or purified.

Because of this very specific procedure, it has completely surprisinglybeen possible to significantly increase both the service life or uselife and hence the operating time of the countercurrent filter apparatusused in the context of the method of the invention and the purifyingaction in relation to the untreated water to be purified. This isbecause, because of the inventive design, with the underlyingcountercurrent principle and the removal and supply, especiallycontinuous removal and supply, of adsorption material, there is, so tospeak, no occurrence of exhaustion of the countercurrent filterapparatus or of the bed present in the countercurrent filter apparatus,which considerably prolongs the operating periods and enables continuousoperation, since the underlying apparatus or plant can effectively beoperated without interruption or time limitation.

More particularly, the contrary or opposing transport of adsorptionmaterial on the one hand and of water to be treated or purified on theother hand (i.e. the contrary flow of the water to be treated orpurified through the bed of the adsorption material or the stream of theadsorption material) significantly increases the filter efficiency inrelation to the removal of the above-cited trace substances ormicrocontaminants, since—without wishing to be restricted to thistheory—the water to be purified or treated is always in contact to somedegree with non-exhausted or regenerated or unladen or fresh adsorptionmaterial. For this reason too, it is possible in accordance with theinvention to achieve high superficial velocities or filtering rates orthroughputs in relation to the water to be treated or purified, suchthat the overall result is an extremely efficient and high-performancemethod according to the invention (which is also enabled in apparatusterms by the specific configuration of the plant of the invention andthe apparatus of the invention), it being possible in this context, aswill be stated hereinafter, to achieve superficial velocities orfiltering rates which may sometimes be more than 50 m/h.

The present invention is based, as stated above, on a procedure ortechnique whereby the adsorbent used or the adsorbents is/are conducted,especially continuously, through the countercurrent filter apparatus orcountercurrent adsorption column used in the context of the method ofthe invention.

Because of the permanent exchange of adsorption material within thecountercurrent filter apparatus, a further advantage of the presentinvention is considered to be that suspended particles or solidparticles that are sometimes present in the untreated water are notcritical. As a result of the continuous or permanent removal ofadsorption material, the bed does not become too dense within theadsorption or countercurrent zone. More particularly, by virtue of thepermanent removal and addition of adsorption material, no interruptionof the water purification is necessary either. More particularly, thereis no need for any complex backflush operations for removal of spentadsorption material.

Moreover, the adsorption material used in accordance with the invention,which is described in detail hereinafter, with the correspondingly highadsorption capacities and the high selectivity, achieves the effect inaccordance with the invention that the amounts of adsorption materialused are relatively low or small, which also enables correspondingregeneration of the adsorption material used on site to some degree, andhence within a single plant having both apparatuses for water treatmenton the one hand and for regeneration of the adsorption material on theother hand. The regeneration of the adsorption material, in the contextof the present invention, is thus integrated into the technologicalconcept and enables development of the overall process on site in theform of a circuit, especially a closed circuit, without the need toreplace significant amounts of adsorption material with new material.

More particularly, the countercurrent filter apparatus of the invention,as also used in the method of the invention, has a small constructionsize, not least because of the use of highly efficient adsorptionmaterial, since the amounts of specific adsorption material are muchlower than the corresponding amounts which have to be used in the caseof prior art purification methods, and since, in relation to thecountercurrent filter apparatuses according to the invention, highfiltering rates result or are enabled by virtue of the construction aswell. As a result of the optimized construction size, the countercurrentfilter apparatus according to the invention, which is used in thecontext of the method of the invention, can be implemented in an overallapparatus or in the purification plant according to the invention with alow space demand overall.

With regard to the present invention, moreover, the term “continuous” asused in the context of the present invention should be understood in avery broad manner, and relates particularly to an embodiment of themethod of the invention whereby especially the addition and withdrawalof the adsorption material to the and from the countercurrent filterapparatus are effected essentially without interruption (in time). Theterm in question, however, also encompasses a procedure whereby thereare interruptions, especially short interruptions, in the addition orwithdrawal of the adsorption material. The same applies to the additionand withdrawal of water, which should especially be effected in asimilarly continuous manner, i.e. essentially without interruption (intime), although there may also be interruptions, especially shortinterruptions, of addition and withdrawal in relation to the water to betreated or purified. With regard to any interruptions, especially shortinterruptions, in the respective transport operations of adsorptionmaterial and water, these may be coordinated independently of oneanother or with respect to one another, or dependently on one another.For example, the transport of water may be stopped, especially for abrief period, for withdrawal or addition of the adsorption material, andvice versa. As stated above, however, an at least essentiallyuninterrupted procedure is preferable in accordance with the invention,both with regard to the adsorption material and the water. Overall, inaccordance with the invention, the method procedure is one which enablesan at least essentially permanent and/or at least essentiallyuninterrupted purification of the water to be treated or purified.

In addition, a further basic idea behind the present invention is tosubject the adsorption material used in the context of the presentinvention, which is, as described hereinafter, especially a specificactivated carbon in grain or bead form, preferably to a regeneration ordesorption, especially a continuous regeneration or desorption,especially a thermal regeneration or desorption, such that adsorptionmaterial which is contaminated or laden with the contaminants and hasbeen withdrawn from the countercurrent filter apparatus is subjected toa regeneration, especially a thermal regeneration, for removal ordesorption of the contaminants adsorbed beforehand, it being possible tofeed the purified adsorption material or the adsorption material freedof contaminants or the unladen or regenerated adsorption materialobtained in this way back to the countercurrent adsorption filtercolumn.

In this way, in accordance with the invention, the performance andefficiency of the method of the invention is increased further,especially associated with a reduction in costs, since the adsorptionmaterial can be recycled or reused to some degree—and without stoppingthe operation of the plant or apparatus of the invention.

Because of the use of specific adsorption materials, especially based onsynthetic raw materials and/or starting materials or preferably based onactivated carbon, especially as defined hereinafter, it is possible toconduct a large number of recycling or regeneration operations with alow material loss, such that the adsorption material used can be usedfor a long period or for numerous purification steps.

On the basis of the withdrawal, envisaged in accordance with theinvention, of adsorption material laden with contaminants from thecountercurrent filter apparatus, and the subsequent regeneration andfeedback into the countercurrent filter apparatus, so to speak, a closedadsorption material circuit with alternating or successive loading ofthe adsorption material on the one hand and regeneration or desorptionof the pollutants or trace substances taken up previously on the otherhand is enabled in the context of the present invention. Similarly,however, it is also possible in principle, in the context of presentinvention, to replace at least a portion of the adsorption material withnew adsorption material, such that a particular proportion of theadsorption material used can be removed from the process cycle—forexample continuously, but also batchwise—and replaced by new adsorptionmaterial.

A further central advantage of the method of the invention is consideredto be that the method according to the invention can be used universallyto some degree, or can be matched individually or tailored in relationto the respective purification requirements. Thus, the method of theinvention can be used for treatment or purification of wastewater,especially communal wastewater, hospital wastewater and industrialwastewater or the like, but also for purification of drinking water.

With regard to the countercurrent filter apparatus used in the contextof the method of the invention, this can especially be configuredaccording to one or more features of the countercurrent filter apparatusof the invention defined hereinafter. In the context of the method ofthe invention, a very specific countercurrent filter apparatus inparticular is thus used, and this, because of its specific apparatusconstruction, enables the contrary transport of water to be treated orpurified on the one hand and adsorption material on the other hand thatunderlies the method of the invention. In this regard, reference mayespecially be made to the remarks which follow in relation to thecountercurrent filter apparatus of the invention.

In this connection, the countercurrent filter apparatus used in thecontext of the method of the invention—in an embodiment preferred inaccordance with the invention—may have at least one housing, saidhousing having at least one adsorption and/or countercurrent zone and atleast one water entry region and at least one water exit region.

More particularly, the adsorption and/or countercurrent zone, in termsof flow, may be disposed between the water entry region and the waterexit region. In addition, the adsorption and/or countercurrent zoneshould be disposed downstream of the water entry region and upstream ofthe water exit region, based on the flow direction of the water.

More particularly, the water entry region should have at least oneadsorption material outlet. In addition, the water exit region shouldhave at least one adsorption material inlet.

Because of this specific apparatus design, the opposing flow or theopposing transport of water to be treated or purified on the one handand adsorption material on the other hand is ensured, especially sincethe water on the one hand and the adsorption material on the other handare introduced into the countercurrent filter apparatus and withdrawntherefrom at different or opposite ends in the countercurrent filterapparatus.

Specifically, the countercurrent filter apparatus which is used in thecontext of the method of the invention should thus firstly have at leastone water entry region, especially having at least one water feed and/orat least one adsorption material outlet, and secondly at least one waterexit region, especially having at least one water drain and/or at leastone adsorption material inlet, and at least one adsorption and/orcountercurrent zone disposed, in terms of flow, between the water entryregion and the water exit region. In the context of the procedure of theinvention, the (untreated) water to be treated or purified is thusconducted through the bed of the adsorption material, especially in theadsorption and/or countercurrent zone of the countercurrent filterapparatus, in countercurrent to the adsorption material to obtaintreated or purified water, followed by removal of the treated orpurified water thus obtained, especially filtrate, from thecountercurrent filter apparatus.

In this connection, the water to be treated, in the context of theprocedure of the invention, should be conducted and/or introduced,especially continuously, into the water entry region, especially throughthe water feed, into the countercurrent filter apparatus. In addition,the treated or purified water, especially the filtrate, should beconducted and/or removed, especially continuously, from thecountercurrent filter apparatus in the water exit region, especiallythrough the water drain.

In this connection, it may likewise be the case in accordance with theinvention that the adsorption material is conducted and/or introducedinto the countercurrent filter apparatus, especially continuously, inthe water exit region, especially through the adsorption material inlet.In this context, the adsorption material should be conducted out ofand/or removed, especially continuously, from the countercurrent filterapparatus in the water exit region, especially through the adsorptionmaterial outlet.

More particularly, in the context of present invention, the water to betreated and/or purified on the one hand and the adsorption material onthe other hand in the countercurrent filter apparatus, especially in theadsorption and/or countercurrent zone, have at least essentiallyopposing flow directions. More particularly, the procedure in accordancewith the invention is such that the water to be treated and/or purifiedon the one hand and the adsorption material on the other hand flowand/or are contacted with one another in opposite directions and/or incountercurrent to one another in the countercurrent filter apparatus,especially in the adsorption and/or countercurrent zone. This results inan efficient removal of the contaminants in question, especially tracematerials or micropollutants, from the (untreated) water to be treatedor purified to obtain the treated or purified water or filtrate, thecontaminants being taken up or adsorbed by the adsorption material.

In the context of a preferred embodiment of the invention, the water tobe treated and/or purified is conducted and/or introduced, especiallycontinuously, into the countercurrent filter apparatus, especially underpressure. More particularly, the water to be treated and/or purifiedshould be conducted and/or introduced into the countercurrent filterapparatus in the water entry region, preferably through the water feed.

More particularly, in the context of the method of the invention, theprocedure is such that the water to be treated or purified which isconducted or introduced into the countercurrent filter column isconducted through an adsorption or countercurrent zone of thecountercurrent filter apparatus disposed downstream of the water entryregion of the countercurrent filter apparatus, based on the flowdirection of the water. In this case, more particularly, the water to betreated and/or purified is contacted with the adsorption material in theadsorption and/or countercurrent zone. More particularly, in accordancewith the invention, the water to be treated and/or purified on the onehand and the adsorption material on the other hand have at leastessentially opposite flow directions. More particularly, the water to betreated or purified on the one hand and the adsorption material on theother hand flow in opposite directions and/or in countercurrent to oneanother in the adsorption and/or countercurrent zone.

According to the invention, more particularly, the procedure is suchthat the water to be treated and/or purified, especially after passingthrough and/or flowing through the adsorption and/or countercurrent zoneof the countercurrent filter apparatus, is conducted out of or removedfrom the countercurrent filter apparatus in a water exit region disposeddownstream of the water entry region of the countercurrent filterapparatus and/or downstream of the adsorption and/or countercurrent zoneof the countercurrent filter apparatus, based on the flow direction ofthe water, especially through a water drain. This is especially thetreated or purified water, or the water or filtrate which has been freedof the contaminants, especially trace materials and/or micropollutants.

In the context of the present invention, because of the specific methodprocedure, especially using a specific purification plant orcountercurrent filter apparatus, high superficial velocities orfiltering rates can be achieved, which significantly increases thefilter efficiency. Thus, in the context of present invention, asuperficial velocity and/or filtering rate, calculated as the quotientof volume flow rate [m³/h] and cross-sectional area [m²] and based onthe water to be treated and/or purified, of at least 10 m/h, especiallyat least 20 m/h, preferably at least 25 m/h, more preferably at least 30m/h, is established in the adsorption and/or countercurrent zone of thecountercurrent filter apparatus.

More particularly, in accordance with the invention, the procedure maybe such that a superficial velocity and/or filtering rate, calculated asthe quotient of volume flow rate [m³/h] and cross-sectional area [m²]and based on the water to be treated and/or purified, in the range from10 m/h to 120 m/h, especially 20 m/h to 100 m/h, preferably 25 m/h to 80m/h, more preferably 30 m/h to 70 m/h, especially preferably 40 m/h to60 m/h, is established in the adsorption and/or countercurrent zone ofthe countercurrent filter apparatus.

With regard to the method of the invention, moreover, more particularly,the adsorption material is fed at least essentially continuously to thecountercurrent filter apparatus. More particularly, the adsorptionmaterial should be conducted at least essentially continuously throughthe countercurrent filter apparatus. In addition, the adsorptionmaterial should be withdrawn at least essentially continuously from thecountercurrent filter apparatus. In this connection, the amount ofadsorption material added per unit time or the volume of adsorptionmaterial added per unit time should correspond at least essentially tothe amount of adsorption material withdrawn per unit time or the volumeof adsorption material withdrawn per unit time. In this way, an at leastessentially constant amount or a constant volume of adsorption materialin the countercurrent filter apparatus and, as a result of this, an atleast essentially constant height of the bed, especially the loose bed,of the adsorption material in the countercurrent filter apparatus isensured.

In addition, the adsorption material should be conducted and/orintroduced into the countercurrent filter apparatus in a water exitregion, preferably through an adsorption material inlet, of thecountercurrent filter apparatus.

More particularly, the adsorption material conducted and/or introducedinto the countercurrent filter column should be conducted through anadsorption and/or countercurrent zone of the countercurrent filterapparatus disposed upstream of the water exit region of thecountercurrent filter apparatus, based on the flow direction of theadsorption material. In this connection, the adsorption material shouldbe contacted in the adsorption and/or countercurrent zone with the waterto be treated and/or purified. More particularly, the adsorptionmaterial on the one hand and the water to be treated and/or purified onthe other hand should have at least essentially opposite flowdirections. In this connection, the adsorption material on the one handand the water to be treated and/or purified on the other hand shouldflow in opposite directions and/or in countercurrent to one anotherand/or be contacted with one another in the adsorption and/orcountercurrent zone.

As stated above, it is particularly advantageous in accordance with theinvention when the adsorption material in the countercurrent filterapparatus, especially in the adsorption and/or countercurrent zone ofthe countercurrent filter apparatus, is in the form of a bed, especiallya loose bed.

In addition, it may be the case in accordance with the invention thatthe adsorption material, especially after passing through and/or flowingthrough the adsorption and/or countercurrent zone of the countercurrentfilter apparatus, is conducted out of and/or removed from thecountercurrent filter apparatus in a water entry region disposeddownstream of the water exit region of the countercurrent filterapparatus and/or downstream of the adsorption and/or countercurrent zoneof the countercurrent filter apparatus, based on the flow direction ofthe adsorption material, especially through an adsorption materialoutlet.

A further central advantage of the procedure of the invention isadditionally that optimized specific mass throughputs can be achieved,in that a relatively small amount of adsorption material leads to alarge volume of purified water or filtrate.

In this connection, it may especially be the case that a specific massthroughput, calculated as the quotient of mass throughput of adsorptionmaterial in the countercurrent filter apparatus [g/h] and volume oftreated and/or purified water and/or filtrate produced [m³], in therange from 10⁻⁷ g/h·m³ to 1000 g/h·m³, especially 10⁻⁶ g/h·m³ to 100g/h·m³, preferably 10⁻⁵ g/h·m³ to 10 g/h·m³, is established.

In addition, it may especially be the case in accordance with theinvention that an exchange (i.e. replacement of adsorption materialladen with contaminants with regenerated or unladen or fresh adsorptionmaterial) in the range from 0.1% to 90% by weight, especially 0.5% to80% by weight, preferably 1% to 70% by weight, more preferably 1.5% to60% by weight, especially preferably 2.5% to 55% by weight, mostpreferably 5% to 50% by weight, is conducted in the countercurrentfilter apparatus, based on the volume of the adsorption material in thebed, especially the loose bed, and based on a period of 24 h. In thisway, it is likewise ensured that non-exhausted or regenerated adsorptionmaterial is present in the bed in a sufficient amount for treatment orpurification of the untreated water. As a result of the continuousexchange of the adsorption material, the bed in the countercurrentfilter column is effectively not exhausted.

With regard to the adsorption material used in the context of the methodof the invention, the adsorption material may be selected from the groupof particulate, especially spherical, adsorption materials. Adsorptionmaterials of this kind have particularly good characteristics in thebed, especially with regard to the flow characteristics of the water tobe treated or purified, but also the transport of the adsorptionmaterial in the bed itself.

More particularly, the adsorption material may be selected from thegroup of

-   -   (i) activated carbon, especially granular activated carbon,        preferably spherical activated carbon and/or especially        activated carbon in the form of PBSAC (polymer-based spherical        activated carbon);    -   (ii) zeolites, especially natural and/or synthetic zeolites;    -   (iii) molecular sieves, especially zeolitic molecular sieves,        synthetic molecular sieves and/or especially synthetic molecular        sieves based on carbon, oxides and/or glasses;    -   (iv) metal oxide and/or metal particles;    -   (v) ion exchange resins, especially polydisperse and/or        monodisperse cation and/or anion exchangers, especially of the        gel type and/or of the macroporous type;    -   (vi) inorganic oxides, especially silicon dioxides, silica gels        and/or aluminum oxides;    -   (vii) porous organic polymers and/or porous organic-inorganic        hybrid polymers and/or porous organic-inorganic hybrid polymers        and/or metal-organic framework materials, especially MOFs        (metal-organic frameworks), COFs (covalent organic frameworks),        ZIFs (zeolite imidazolate frameworks), POMs (polymer organic        materials) and/or OFCs;    -   (viii) mineral granulates;    -   (ix) clathrates; and    -   (x) mixtures and/or combinations thereof.

In a manner which is preferable in accordance with the invention, theadsorption material may be formed from activated carbon, especially fromgranular, preferably spherical, activated carbon.

The respective adsorption materials which can be used in the context ofthe method of the invention are well known as such to those skilled inthe art, and the person skilled in the art is capable at any time ofselecting the particular adsorption material in the light of theprocedure of the invention in accordance with the present details,especially for assurance of a high adsorption efficiency and theregeneration, especially the thermal regeneration, envisaged inaccordance with the invention.

Activated carbons usable in accordance with the invention, which canespecially be used on the basis of particulate or spherical activatedcarbon, are obtainable, for example, from Blucher GmbH, Erkrath,Germany, or from Adsor-Tech GmbH, Premnitz, Germany. In addition, inrelation to the activated carbon usable in accordance with theinvention, reference may be made to the applicant's own European patentapplication EP 1 918 022 A1 and to the parallel US 2008/017589 A1, therespective disclosures of which are hereby fully incorporated byreference. More particularly, the activated carbon used in accordancewith the invention can be obtained by carbonization of startingmaterials or polymers, especially synthetic starting materials orpolymers, with subsequent activation. The activated carbon used inaccordance with the invention can be obtained, for example, bycarbonization and subsequent activation of sulfonatedstyrene/divinylbenzene copolymers in gel form, especially sulfonateddivinylbenzene-crosslinked polystyrenes, in grain form, preferably inbead form.

In addition, for further details of the MOF materials usable inaccordance with the invention, reference may be made particularly tointernational patent application WO 2009/096184 A1 and the parallelGerman patent application DE 10 2008 005 218 A1, the respectivedisclosures of which are hereby fully incorporated by reference.

The adsorption materials used in accordance with the invention,especially activated carbons, as well as their excellent physicalproperties (i.e. high mechanical stability, low abrasion and low dustformation and, as a result, excellent transport properties both withinthe bed and in the context of the regeneration process), additionallyalso have excellent adsorption properties with regard to thecontaminants to be removed from the water to be treated or purified.More particularly, in the context of present invention, it is possibleto use an activated carbon which has been tailored to some degree, whichtakes account of the complexity, the molecule sizes, and the specificpolarities of the contaminants or micropollutants to be removed and theway that it influences the adsorption characteristics. Moreparticularly, especially taking account of the polarities and thehydrate shells of the molecule size that result in the water phase,great significance attaches to the contaminants to be removed, in that avery specific adsorption pore system with a matched specific surfacechemistry of the adsorption material or of the activated carbon used isadvantageous for optimum adsorption. As stated above, it is possible toindividually match or tailor the adsorption materials or activatedcarbons used in the context of the present invention to some degree inthis regard, which leads to further optimization of the adsorptionproperties. As a result, significant advantages also result overconventional adsorption materials, especially with regard to adsorptionperformance, selectivity and the associated use times, which also leadsto reduced costs overall.

More particularly, the adsorption material used in the context of themethod of the invention, especially the preferably particulate activatedcarbon, may have a monodisperse particle size distribution or aheterodisperse particle size distribution.

In the context of the present invention, it is additionally preferablethat the adsorption material, especially the preferably particulateactivated carbon, has particle sizes, especially particle diameters, inthe range from 0.001 to 5 mm, especially 0.005 to 3 mm, preferably 0.01to 2 mm, more preferably 0.015 to 1.5 mm, most preferably 0.05 to 1 mm.

More particularly, the adsorption material, especially the preferablyparticulate activated carbon, has mean particle sizes, especially medianparticle diameters (D50), in the range from 0.01 to 2 mm, especially0.05 to 1.5 mm, preferably 0.1 to 1 mm.

The corresponding particle sizes or diameters can especially bedetermined on the basis of the method according to ASTM D2862-97/04.

The selection of specific particle sizes or particle diameters leads, inthe light of the present invention, firstly to a particularlyhomogeneous bed within the countercurrent filter apparatus and toimproved transport properties of the activated carbon material,especially in the context of recycling or regeneration, but also in thecontext of the (transport) characteristics of the adsorption material inthe bed, especially in the loose bed. Secondly, the particle sizesspecified lead to a further improvement in the flow characteristics ofthe water in the bed.

In addition, the adsorption material, especially the preferablyspherical activated carbon, should have an abrasion resistance (ball panhardness) or abrasion hardness of at least 90%, especially at least 95%,preferably at least 97%, more preferably at least 98%, most preferablyat least 99%. The abrasion resistance is especially determined to ASTMD3802-05. The high abrasion resistance leads to low abrasion of theactivated carbon, especially in the context of the underlying transportprocesses, which likewise prolongs the duration of use.

In this connection, the adsorption material, especially the preferablyparticulate activated carbon, should have a compressive strength orbursting resistance (weight durability) per adsorption particle,especially per activated carbon particle, of at least 5 newtons,especially at least 10 newtons, preferably at least 20 newtons. Moreparticularly, the adsorption material, especially the preferablyparticulate activated carbon, should have a compressive strength orbursting resistance (weight durability) per adsorption particle,especially per activated carbon particle, in the range from 10 to 50newtons, especially 12 to 45 newtons, preferably 15 to 40 newtons.

In the context of present invention, it is likewise advantageous whenthe adsorption material, especially the preferably particulate activatedcarbon, is at least essentially dust-free. This prevents, for example,any sludge formation in the countercurrent filter apparatus.

Equally, the adsorption material, especially the preferably particulateactivated carbon, should have an ash content of not more than 1% byweight, especially not more than 0.8% by weight, preferably not morethan 0.6% by weight, more preferably not more than 0.5% by weight,especially preferably not more than 0.2% by weight. The ash content isespecially determined to ASTM D2866/94-04.

The adsorption material, especially the preferably particulate activatedcarbon, should have a surface oxygen content of not more than 10% byweight, especially not more than 8% by weight, preferably not more than6% by weight, more preferably not more than 5% by weight. In addition,the adsorption material, especially the preferably particulate activatedcarbon, should be hydrophobic and/or have hydrophobic surfaceproperties.

The surface oxygen content can especially be determined by means of theESCA method (electron spectroscopy for chemical analysis).

More particularly, the adsorption material, especially the preferablyparticulate activated carbon, should have a specific surface area (BETsurface area) of at least 500 m²/g, especially at least 750 m²/g,preferably at least 1000 m²/g, especially preferably at least 1200 m²/g.More particularly, the adsorption material, especially the preferablyparticulate activated carbon, should have a specific surface area (BETsurface area) in the range from 500 to 4000 m²/g, especially 750 to 3000m²/g, preferably 1000 to 2500 m²/g, especially preferably 1100 to 2000m²/g.

The determination of the specific BET surface area is known in principleto those skilled in the art. All BET surface area figures given relateespecially to the determination to ASTM D6556-04. In the context of thepresent invention, the BET surface area is especially determined by whatis called the multipoint BET determination method (MP-BET) within apartial pressure range p/p₀ from 0.05 to 0.1.

In addition, the adsorption material, especially the preferablyparticulate activated carbon, should have an adsorption volume V_(ads)of at least 250 cm³/g, especially at least 300 cm³/g, preferably atleast 350 cm³/g, especially preferably 400 cm³/g. More particularly, theadsorption material, especially the preferably particulate activatedcarbon, should have an adsorption volume V_(ads) in the range from 250to 3000 cm³/g, especially 300 to 2000 cm³/g, preferably 350 to 2500cm³/g.

The adsorption volume V_(ads) is a parameter well known to those skilledin the art for characterization of the particulate adsorption materialsused. The determination methods for this purpose are also well known perse to those skilled in the art. More particularly, the adsorption volumeV_(ads) is the volume of N₂ adsorbed based on weight, which is generallydetermined at a partial pressure p/p₀ of 0.995.

In addition, the adsorption material, especially the preferablyparticulate activated carbon, should have a total pore volume accordingto Gurvich of at least 0.50 cm³/g, preferably at least 0.55 cm³/g, morepreferably 0.60 cm³/g, especially preferably at least 0.65 cm³/g, mostpreferably 0.70 cm³/g. In this connection, the adsorption material,especially the preferably particulate activated carbon, should have atotal pore volume according to Gurvich in the range from 0.50 to 2.0cm³/g, especially 0.55 to 1.5 cm³/g, preferably 0.60 to 1.2 cm³/g,especially preferably 0.65 to 1.0 cm³/g.

With regard to the determination of total pore volume according toGurvich, this is a measurement or determination method known per se tothose skilled in the art in this field. For further details regardingthe determination of the total pore volume according to Gurvich,reference may be made, for example, to L. Gurvich (1915), J. Phys. Chem.Soc. Russ. 47, 805, and to S. Lowell et al., Characterization of PorousSolids and Powders: Surface Area Pore Size and Density, Kluwer AcademicPublishers, Article Technologies Series, pages 111 ff.

In addition, the adsorption material, especially the preferablyparticulate activated carbon, may have a total porosity in the rangefrom 10% to 80%, especially 20% to 75%, preferably 25% to 70%, based onthe total volume of the adsorption material. In addition, the adsorptionmaterial, especially the preferably particulate activated carbon, mayhave a specific total pore volume in the range from 0.01 to 4.0 cm³/g,especially 0.1 to 3.0 cm³/g, preferably 0.2 to 2.0 cm³/g. In particular,the proportion of pores having pore diameters of ≤75 Å may be at least65%, especially at least 70%, preferably at least 75%. In addition, theadsorption material, especially the preferably particulate activatedcarbon, based on the total pore volume, especially on the total porevolume according to Gurvich, may have a proportion of micropores,especially of micropores having pore diameters of ≤30 Å, especially of≤25 Å, preferably of ≤20 Å, of at least 70%, especially at least 75%,preferably at least 80%, more preferably at least 85%, especiallypreferably at least 90%.

The micropore volume can especially be determined by the carbon blackmethod. The carbon black determination method is known per se to thoseskilled in the art, and so there is no need for any further details inthis regard. In addition, for further details of the determination ofthe pore surface area and the pore volume by the carbon black method,reference may be made to R. W. Magee, Evaluation of the External SurfaceArea of Carbon Black by Nitrogen Adsorption, Presented at the Meeting ofthe Rubber Division of the American Chem. Soc., October 1994,referenced, for example, in: Quantachrome Instruments, AUTO-SORB-1, AS1WinVersion 1.50, Operating Manual, OM, 05061, Quantachrome Instruments2004, Florida, USA, pages 71 ff.

In addition, the adsorption material, especially the preferablyparticulate activated carbon, should have an iodine number of at least1000 mg/g, especially at least 1250 mg/g, preferably at least 1500 mg/g.More particularly, the adsorption material, especially the preferablyparticulate activated carbon, should have an iodine number in the rangefrom 1000 to 2100 mg/g, especially 1250 to 2050 mg/g, preferably 1500 to2000 mg/g. The iodine number is especially determined to ASTMD4607-94/99.

Finally, the adsorption material, especially the preferably particulateactivated carbon, should have a bulk density in the range from 250 to700 g/L, especially 300 to 625 g/L, preferably 300 to 600 g/L, morepreferably 350 to 550 g/L, the bulk density being determined especiallyto ASTM B527-93/00. The bulk densities envisaged in accordance with theinvention likewise lead to optimized behavior of the adsorptionmaterial, especially in the loose bed, accompanied by optimized flowcharacteristics of the water to be treated or purified in the bed.

As stated above, the adsorption material laden with the contaminantswhich is used in accordance with the invention can be subjected to aregeneration, especially a thermal regeneration, to obtain an unladen orregenerated or fresh adsorption material which can be fed back to thecountercurrent filter apparatus on completion of regeneration.

Against this background, reference is made hereinafter to particularembodiments and details relating to the regeneration of the adsorptionmaterial.

In this connection, it is particularly advantageous in the context ofthe present invention when the adsorption material conducted out ofand/or removed from the countercurrent filter apparatus, especially theadsorption material laden with the contaminants, is dried and/orsubjected to a regeneration and/or recycling operation, especially acontinuous and/or especially a thermal regeneration and/or recyclingoperation, and optionally subsequently remoistened. For this purpose, itis especially possible to use a regeneration apparatus which may be partof the purification plant of the invention as defined hereinafter andwhich especially comprises:

-   -   optionally at least one drying and/or demoistening unit for        drying and/or demoistening the adsorption material conducted out        of and/or removed from the countercurrent filter apparatus        and/or the adsorption material laden with the contaminants,        especially wherein the drying and/or demoistening unit is        disposed downstream of the countercurrent filter apparatus,        based on the transport direction of the adsorption material,    -   at least one regeneration and/or desorption unit or apparatus,        especially for preferably thermal regeneration of the adsorption        material conducted out of and/or removed from the countercurrent        filter apparatus and/or of the adsorption material laden with        contaminants and/or for provision of regenerated and/or unused        adsorption material, especially wherein the regeneration and/or        desorption unit is disposed downstream of the countercurrent        filter apparatus and/or downstream of the drying and/or        demoistening apparatus and/or especially wherein the        regeneration and/or desorption unit is disposed upstream of the        countercurrent filter apparatus, based in each case on the        transport direction of the adsorption material,    -   optionally at least one moistening unit or apparatus, especially        for moistening of regenerated and/or unused adsorption material,        especially wherein the moistening unit is disposed downstream of        the regeneration and/or desorption unit and/or especially        wherein the moistening unit is disposed upstream of the        countercurrent filter apparatus, based in each case on the        transport direction of the adsorption material.

More particularly, in the context of the present invention, it may bethe case that the adsorption material conducted out of and/or removedfrom the countercurrent filter apparatus and/or the adsorption materialladen with the contaminants is dried, especially using the drying and/ordemoistening unit. In this connection, the residual moisture content ofthe dried adsorption material may be adjusted to a value of not morethan 1% by weight, especially not more than 0.5% by weight, preferablynot more than 0.2% by weight, based on the adsorption material. Theresidual water obtained in the context of the demoistening may, forexample, be fed back to the countercurrent filter apparatus as untreatedwater.

This drying operation may be divided into predrying and/or main dryingsteps, especially successive predrying and/or main drying steps. Moreparticularly, in the context of the drying, especially predrying, it ispossible, for example, to use inclined clarifiers and/or belt driers. Inaddition, in the context of the drying, especially main drying, it ispossible to use belt driers and/or fluidized bed driers. Moreparticularly, the feeding and/or transport of the adsorption material(i.e. adsorption material suspended in residual water), especially inthe form of a suspension, can be fed to the aforementioned drying and/ordemoistening units via pipelines using corresponding pump apparatusesand/or suspension conveying apparatuses, especially jet pumps and/orperistaltic pumps.

In addition, the adsorption material conducted out of and/or removedfrom the countercurrent filter apparatus, especially on completion ofdrying, preferably as defined above, is subjected to a regenerationand/or desorption, especially a thermal regeneration and/or desorption,especially with release and/or desorption of the contaminants adsorbedin the adsorption material, especially using the regeneration and/ordesorption unit. In this connection, the procedure is especially suchthat the contaminants present in the adsorption material are desorbedand/or the regenerated or unladen or fresh adsorption material isobtained.

More particularly, the optionally dried adsorption material, usingsuitable conveying apparatuses, such as a vibrating channel, a conveyingapparatus, especially a pneumatic conveying apparatus, and/or a beltapparatus can be fed to the regeneration and/or desorption unit. Theregeneration and/or desorption unit, in accordance with the invention,is especially a preferably indirectly heated rotary oven, ahigh-temperature fluidized bed apparatus and/or a microwave oven. As aresult of the desorption, which is especially a thermal desorption, onthe basis of which the contaminants are removed from or driven out ofthe adsorption material with the aid of thermal energy, a desorbed orregenerated or unused or fresh adsorption material is obtained.

In the context of the regeneration of the adsorption material, inaccordance with the invention, the procedure may especially be such thatthe adsorption material is heated, especially in the regeneration and/ordesorption unit, to temperatures in the range from 150° C. to 1000° C.,especially 200° C. to 950° C., preferably 250° C. to 900° C., morepreferably 250° C. to 500° C., especially for a period of 1 min to 300min, especially 10 min to 200 min. In this connection, the heating maybe conducted under an inert gas atmosphere or under an at most slightlyoxidizing atmosphere.

With regard to the contaminants removed from the adsorption material,the contaminants released and/or desorbed in this way may be sent to athermal final utilization, especially incineration, in which case it ispossible to use the incineration apparatuses known per se to thoseskilled in the art for this purpose.

In the context of the regeneration, especially the thermal regeneration,it may likewise be the case in accordance with the invention that theregenerated or fresh adsorption material is cooled or introduced intoand/or stored intermediately in a reservoir unit or apparatus. In thisconnection, the transport of the adsorption material freed of thecontaminants, proceeding from the regeneration or desorption unit intothe reservoir apparatus, can be effected using the apparatuses citedabove for the transport of the adsorption material from the dryingapparatus to the regeneration or desorption unit. The storage ofregenerated or unladen or fresh adsorption material, especially in thereservoir apparatus cited above, is associated with the advantage thatthe volume of regenerated or unladen or fresh adsorption materialconducted into the countercurrent filter apparatus again can be adjustedor dosed as required.

In addition, in the context of present invention, the procedure may besuch that the regenerated or unladen or fresh adsorption material ismoistened using the moistening unit in particular and/or introduced intowater. In this regard, it is possible to use corresponding conveying ormoistening units, for example jet pumps and/or peristaltic pumps. Inthis way, it is especially possible to obtain a preferably aqueoussuspension of the regenerated or unused or fresh adsorption material.For the moistening of the adsorption material, it is especially possibleto use corresponding untreated water. The conveying or moistening unitsmay likewise or simultaneously be used for transport of the adsorptionmaterial to or into the countercurrent filter apparatus, especially ifthe latter comprises jet pumps or peristaltic pumps.

The regenerated or unladen or fresh and preferably moistened adsorptionmaterial obtained in this way can subsequently be conducted orintroduced back into the countercurrent filter apparatus, especiallyunder pressure, preferably via corresponding pipelines connected to theadsorption material inlet of the countercurrent apparatus.

If corresponding pump units, for example based on jet pumps and/orperistaltic pumps, are used for transport of the adsorption material,especially in the form of a preferably aqueous dispersion, the motivewater in this regard may likewise be taken from the untreated water.

The pump apparatuses used may likewise be used for moistening of theadsorption material.

With regard to the method of the invention, moreover, the methodaccording to the invention may be conducted with a circulation factor,calculated as the quotient of the amount of the adsorption material [kg]present in the regeneration and/or recycling, especially in theregeneration apparatus, and the amount of the adsorption material [kg]present in the countercurrent filter apparatus in the range from 0.1 to100, especially 0.5 to 75, preferably 0.75 to 50, more preferably 1 to40, especially preferably 1.25 to 30. In the context of the presentinvention, the procedure may thus be such that a relatively highproportion of adsorption material is present in the countercurrentfilter apparatus, especially in the form of the preferably loose bed,and is used as such for the purposes of purifying the untreated water,which constitutes a method-specific optimization. The circulation factorcan especially be calculated by the general formulaF_(U)=m_(ads,DP)/m_(ads,AP) (with F_(U): circulation factor; m_(ads,DP):mass or amount of the adsorption material in the regeneration and/ordesorption process; m_(ads,AP): mass or amount of the adsorptionmaterial in the countercurrent filter apparatus).

The present invention likewise relates, in this aspect of the presentinvention, to a method for treatment and/or purification of water,especially of wastewater or drinking water, preferably for adsorptiveremoval of inorganic- or organic-based, especially organic-based,contaminants such as trace substances and/or micropollutants. The methodis especially conducted as defined above, wherein water to be treatedand/or purified, for the purposes of treatment and/or purification, iscontacted with an adsorption material, especially a particulateadsorption material, wherein the adsorption material is disposed in abed, especially in a loose bed, in a countercurrent filter apparatus,especially a countercurrent adsorption filter column, and the water tobe treated and/or purified flows through it for adsorptive removal ofthe contaminants. In addition, the adsorption material of the beddisposed in the countercurrent filter apparatus is removed andregenerated, especially in a continuous manner, in countercurrent to theflow of the water to be treated and/or purified. In this context,moreover, regenerated and/or unused adsorption material, preferablyregenerated adsorption material, is fed in countercurrent to the streamof the water to be treated and/or purified in amounts at leastessentially equal to that of adsorption material removed from the bed.

More particularly, the method of the invention can also be conductedusing the purification plant according to the invention as definedhereinafter, which may comprise a regeneration apparatus and thecountercurrent filter apparatus according to the invention.

As stated above, the method of the invention is described in more detailby the further independent method claims and dependent claims in thisregard, and by reference to the descriptions of the figures.

The present invention further relates—in a further aspect of the presentinvention—to the purification plant of the invention, preferably fortreatment and/or purification of water, especially of wastewater ordrinking water, preferably for adsorptive removal of inorganic- ororganic-based, especially organic-based, contaminants such as tracesubstances and/or micropollutants, wherein the plant includes

-   -   at least one countercurrent filter apparatus, especially        countercurrent adsorption filter column, for treatment of water        and for uptake, storage and release, especially continuous        uptake, storage and release, of at least one preferably        particulate adsorption material, and    -   at least one regeneration apparatus for withdrawal, especially        continuous withdrawal, of adsorption material laden with the        contaminants from the countercurrent filter apparatus,        regeneration and/or recycling of adsorption material laden with        the contaminants and feeding of regenerated or unused adsorption        material back into the countercurrent filter apparatus,        wherein the regeneration apparatus, for regeneration and reuse,        especially continuous regeneration and reuse, of the adsorption        material is connected to the countercurrent filter apparatus in        such a way that, in the operating state and/or use state of the        purification plant, the water to be treated and/or purified and        the adsorption material are conducted in countercurrent and/or        in opposite directions to one another in the countercurrent        filter plant.

The purification plant of the invention is especially suitable for usein the context of the above-described method according to the invention.More particularly, the purification plant of the invention enables theprinciple of the invention, whereby the adsorption material on the onehand and the water to be treated or purified on the other hand areconducted in countercurrent to one another for the purpose of purifyingthe water or removing contaminants such as trace substances ormicropollutants from the water. In addition, the purification plant ofthe invention enables simultaneous purification of untreated water andregeneration of the adsorption material with the respective recycling ofregenerated adsorption material for further purification orrepurification of untreated water, so as to provide, overall, ahigh-performance purification plant according to the invention, whichenables the implementation of all the method aspects of the presentinvention with a low space demand and inexpensive operation. Moreparticularly, the purification plant of the invention enables optimizedcirculation factors since a high proportion of the adsorption materialpresent in the plant overall can be used for the purposes of purifyinguntreated water. On the basis of the specific inventive technical designof the purification plant according to the invention, in addition, highspecific mass throughputs are possible, since, based on the amount ofsorption material used, large amounts or volumes of purified water orfiltrate are obtained. Finally, the purification plant of the inventionenables efficient purification of untreated water, with prevention ofbreakthroughs of the contaminants in question particularly because ofthe use of a specific countercurrent filter apparatus, especially asdefined hereinafter, thus making it possible to obtain a high-purityfiltrate, which is of high significance particularly also for provisionof drinking water.

For further details in this regard relating to the purification plant ofthe invention, as stated above, reference may be made to thecorresponding further independent claims and to the dependent claimsthat relate to the purification plant of the invention, and thecorresponding descriptions of the figures.

Furthermore, the present invention—in a further aspect of the presentinvention—relates to the countercurrent filter apparatus of theinvention, especially countercurrent adsorption filter column,preferably continuous countercurrent adsorption filter column,preferably for treatment and/or purification of water, especially ofwastewater or drinking water, preferably for adsorptive removal ofinorganic- or organic-based, especially organic-based, contaminants suchas trace substances and/or micropollutants, and for uptake, storage andrelease, preferably continuous uptake, storage and release, of at leastone preferably particulate adsorption material,

-   -   wherein the countercurrent filter apparatus has at least one        housing, said housing having at least one adsorption and/or        countercurrent zone and at least one water entry region and at        least one water exit region,    -   wherein the adsorption and/or countercurrent zone, in terms of        flow, is disposed between the water entry region and the water        exit region and/or wherein the adsorption and/or countercurrent        zone is disposed downstream of the water entry region and        upstream of the water exit region, based on the flow direction        of the water, and    -   wherein the water entry region has at least one adsorption        material outlet and wherein the water exit region has at least        one adsorption material inlet.

Because of the specific apparatus configuration of the countercurrentfilter apparatus according to the invention, it is firstly possible toimplement the principle of the opposite transport of untreated water onthe one hand and adsorption material on the other hand that underliesthe present invention in the countercurrent filter apparatus. Secondly,the countercurrent filter apparatus of the invention enables, withsimultaneously high purification of the untreated water, highsuperficial velocities or filtering rates, which leads to highthroughputs of untreated water and the obtaining of large amounts ofpurified filtrate.

In addition, the filter apparatus of the invention is notable for acompact and hence space-saving construction, especially also with regardto the adsorption or countercurrent zone. As explained hereinafter, theadsorption or countercurrent zone may have a smaller diameter or asmaller cross-sectional area than the corresponding water entry and exitregions of the filter apparatus of the invention, which equally allowsor leads to an increase in the superficial velocity or filtering rate;wherein, in a preferred embodiment of the invention and as citedhereinafter, specific transition regions are disposed between theadsorption and/or countercurrent zone and the water entry region or thewater exit region, and this leads to optimization of the respectivetransport processes of water and adsorption material in terms of flow.

In this connection, the inventive principle of the opposite transport ofuntreated water and adsorption material is also conducive to highsuperficial velocities or filtering rates, since regenerated or unladenor fresh adsorption material is always being fed to the actualpurification process to some degree in accordance with the invention,which enables high through-flow rates or flow velocities in relation tothe untreated water with simultaneously efficient purification(avoidance of breakthroughs of trace materials or micropollutants).

For further details relating to the countercurrent filter apparatus ofthe invention, as stated above, reference may be made to thecorresponding dependent apparatus claims and the correspondingdescriptions of the figures. Finally, the present invention relates—in afurther aspect of the present invention—to the use of a purificationplant, especially as defined in the present context, or of acountercurrent filter apparatus, especially as defined in the presentcontext, or of adsorption material, especially as defined in the presentcontext, in a method for treatment or purification of water, especiallyof wastewater or drinking water, preferably for adsorptive removal ofinorganic- or organic-based, especially organic-based, contaminants,especially as defined in the present context.

The present invention is elucidated in detail hereinafter with referenceto preferred working examples or drawings or figures that representembodiments. In connection with the elucidation of these preferredworking examples of the present invention, although these are notrestrictive in any way in relation to the present invention, furtheradvantages, properties, aspects and features of the present inventionare also indicated.

The figures show:

FIG. 1 a schematic diagram or overview of the purification plant A ofthe invention, preferably for treatment or purification of water oruntreated water AW, preferably for adsorptive removal of inorganic- ororganic-based, especially organic-based, contaminants such as tracematerials and/or micropollutants, in one embodiment of the invention;

FIG. 2 a schematic section diagram of the countercurrent filterapparatus 1 of the invention, especially countercurrent adsorptionfilter column, in a preferred embodiment of the invention, wherein thecountercurrent filter apparatus 1 has at least one housing 2, saidhousing 2 having at least one adsorption and/or countercurrent zone 3and at least one water entry region 4 and at least one water exit region5, and wherein the water entry region 4 has at least one adsorptionmaterial outlet 6 and wherein the water exit region 5 has at least oneadsorption material inlet 7;

FIG. 3 a further schematic section diagram of the countercurrent filterapparatus 1 of the invention, especially countercurrent adsorptionfilter column, in a preferred embodiment of the invention and with anillustration of the flow or transport of the water W on the one hand andthe adsorption material AK on the other hand that is present in thecountercurrent filter apparatus 1, so of the bed 15, especially theloose bed 15, of the adsorption material present in the countercurrentfilter apparatus.

FIG. 1 is a schematic diagram of a preferred embodiment of thepurification plant of the invention, as defined in further detailhereinafter:

More particularly, FIG. 1 shows the purification plant A of theinvention, preferably for treatment and/or purification of water AW,especially of wastewater or drinking water, preferably for adsorptiveremoval of inorganic- or organic-based, especially organic-based,contaminants such as trace substances and/or micropollutants, whereinthe plant A includes

-   -   at least one countercurrent filter apparatus 1, especially        countercurrent adsorption filter column, for treatment and/or        purification of water AW and for uptake, storage and release,        especially continuous uptake, storage and release, of at least        one preferably particulate adsorption material, and    -   at least one regeneration apparatus RV for withdrawal,        especially continuous withdrawal, of adsorption material laden        with the contaminants from the countercurrent filter apparatus        1, regeneration and/or recycling of adsorption material laden        with the contaminants and feeding of regenerated and/or unladen        and/or fresh adsorption material back into the countercurrent        filter apparatus 1,        wherein the regeneration apparatus RV, for regeneration and        reuse, especially continuous regeneration and reuse, of the        adsorption material is connected to the countercurrent filter        apparatus 1 in such a way that, in the operating state and/or        use state of the plant A, the water AW to be treated and/or        purified and the adsorption material are conducted in        countercurrent and/or in opposite directions to one another in        the countercurrent filter apparatus 1.

The present invention likewise relates to a purification plant A asshown in FIG. 1, preferably for treatment and/or purification of waterAW, especially of wastewater or drinking water, preferably foradsorptive removal of inorganic- or organic-based, especiallyorganic-based, contaminants such as trace substances and/ormicropollutants, wherein the plant (A) includes:

-   -   at least one countercurrent filter apparatus, especially        countercurrent adsorption filter column, for treatment of water        AW and for uptake, storage and release, especially continuous        uptake, storage and release, of at least one preferably        particulate adsorption material, especially as defined above,        especially wherein, in the operating state and/or use state, the        water AW to be treated and/or purified and the adsorption        material are conducted in countercurrent and/or in opposite        directions to one another in the countercurrent filter apparatus        1, and    -   optionally at least one drying and/or demoistening unit T1, T2,        T3 for drying and/or demoistening of adsorption material laden        with the contaminants, especially wherein the drying and/or        demoistening unit T1, T2, T3 is disposed downstream of the        countercurrent filter apparatus 1, based on the transport        direction of the adsorption material,    -   at least one regeneration and/or desorption unit R, especially        for regeneration of adsorption material laden with the        contaminants and/or for provision of regenerated and/or unladen        and/or fresh adsorption material, especially wherein the        regeneration and/or desorption unit R is disposed downstream of        the countercurrent filter apparatus 1 and/or downstream of the        drying and/or demoistening unit T1, T2, T3 and/or especially        wherein the regeneration and/or desorption unit R is disposed        upstream of the countercurrent filter apparatus 1, based in each        case on the transport direction of the adsorption material,    -   optionally at least one moistening unit B, especially for        moistening of regenerated and/or unladen and/or fresh adsorption        material, especially wherein the moistening unit B is disposed        downstream of the regeneration and/or desorption unit R and/or        especially wherein the moistening unit B is disposed upstream of        the countercurrent filter apparatus, based in each case on the        transport direction of the adsorption material.

More particularly, the present invention also relates to a purificationplant A as shown in FIG. 1, preferably for treatment and/or purificationof water AW, especially of wastewater or drinking water, preferably foradsorptive removal of inorganic- or organic-based, especiallyorganic-based, contaminants such as trace substances and/ormicropollutants, wherein the plant A includes:

-   -   at least one countercurrent filter apparatus 1, especially        countercurrent adsorption filter column, for treatment and/or        purification of water AW and for uptake, storage and release,        especially continuous uptake, storage and release, of at least        one preferably particulate adsorption material, especially as        defined above, especially wherein, in the operating state and/or        use state, the water AW to be treated and/or purified and the        adsorption material are conducted in countercurrent and/or in        opposite directions to one another in the countercurrent filter        apparatus,    -   wherein the countercurrent filter apparatus 1 has at least one        housing 2, said housing 2 having at least one adsorption and/or        countercurrent zone 3 and at least one water entry region 4 and        at least one water exit region 5,    -   wherein the adsorption and/or countercurrent zone 3, in terms of        flow, is disposed between the water entry region 4 and the water        exit region 5 and/or wherein the adsorption and/or        countercurrent zone 3 is disposed downstream of the water entry        region 4 and upstream of the water exit region 5, based on the        flow direction of the water, and    -   wherein the water entry region 4 has at least one adsorption        material outlet 6 and wherein the water exit region 5 has at        least one adsorption material inlet 7,    -   optionally at least one drying and/or demoistening unit T1, T2,        T3 for drying and/or demoistening of adsorption material laden        with the contaminants, especially wherein the drying and/or        demoistening unit T1, T2, T3 is disposed downstream of the        countercurrent filter apparatus 1, based on the transport        direction of the adsorption material,    -   at least one regeneration and/or desorption unit R, especially        for regeneration of adsorption material laden with the        contaminants and/or for provision of regenerated and/or unladen        and/or fresh adsorption material, especially wherein the        regeneration and/or desorption unit R is disposed downstream of        the countercurrent filter apparatus 1 and/or downstream of the        drying and/or demoistening unit T1, T2, T3, based in each case        on the transport direction of the adsorption material,    -   optionally at least one moistening unit B, especially for        moistening of regenerated and/or unused adsorption material,        wherein the moistening unit B is disposed downstream of the        regeneration and/or desorption unit R, based on the transport        direction of the adsorption material.

With regard to the drying and/or demoistening plant T1, T2, T3 of thepurification plant of the invention, as defined above, the latter may beselected from the group of belt driers, fluidized bed driers andinclined clarifiers and combinations thereof. More particularly, thedrying and/or demoistening unit T1, T2, T3 may comprise at least onemain drying and/or main demoistening unit T2, T3, especially selectedfrom belt driers and/or fluidized bed driers, and optionally at leastone predrying and/or predemoistening unit T1, T2, especially selectedfrom inclined clarifiers and belt driers. In this connection, thepredrying and/or predemoistening unit T1, T2 should be disposed upstreamof the main drying and/or main demoistening unit T2, T3, based on thetransport direction of the adsorption material.

According to the invention, it may additionally be the case that therespective drying and/or demoistening units T1, T2, T3 are eachindependently equipped with recycle units for transporting withdrawnresidual water away, especially for feeding and/or recycling theresidual water back into the water flow and/or stream W, preferably forrecycling into the water entry region 8 of the countercurrent filterapparatus 1.

More particularly, the drying and/or demoistening unit T1, T2, T3 may beconnected to the adsorption material outlet 6 of the countercurrentfilter apparatus 1, especially by means of a pipeline through which theadsorption material, especially provided with residual water and presentin a suspension, is transported.

In addition, the regeneration and/or desorption unit R may be selectedfrom the group of rotary ovens, especially indirectly heated rotaryovens; belt ovens, especially indirectly heated belt ovens; fluidizedbed driers, especially high-temperature fluidized bed driers; andmicrowave ovens.

With regard to the regeneration and/or desorption unit R, moreover, thelatter may additionally include means and/or units for transporting awayand/or for further treatment, especially for thermal decomposition, ofdesorbed contaminants and/or contaminants released from the adsorptionmaterial.

In the context of the present invention, it may be the case that thedrying and/or demoistening unit T1, T2, T3, especially the main dryingand/or main demoistening unit T2, T3, preferably the main drying and/ormain demoistening unit T3, is connected to the regeneration and/ordesorption unit R, especially by means of a pipeline, an agitatedtransport unit, a conveying unit, especially a pneumatic conveying unit,and/or a belt transport unit. In this way, the dried adsorption materialcan be conducted to the regeneration or adsorption unit.

More particularly, the adsorption material outlet 6 of thecountercurrent filter apparatus may be connected to the regenerationand/or desorption unit R, especially by means of a pipeline, especiallyin the case, which is less preferred in accordance with the invention,of the procedure without a drying and/or demoistening unit T1, T2, T3.

More particularly, the moistening unit (B) may be selected from thegroup of stirred tanks, spray towers, belt moisteners, (water-)jetpumps, peristaltic pumps and combinations thereof.

In addition, the purification plant A according to the invention mayalso include at least one reservoir unit V, especially for storageand/or intermediate storage of regenerated and/or unladen and/or freshadsorption material. In this connection, the reservoir unit V may bedisposed downstream of the regeneration and/or desorption unit R and/orupstream of the moistening unit B, based on the transport direction ofthe adsorption material.

With regard to the regeneration and/or desorption unit R, moreover, thelatter may be connected to the reservoir unit V and/or the moisteningunit B, especially by means of a pipeline, an agitated transport unit, aconveying unit, especially a pneumatic conveying unit, and/or a belttransport unit. More particularly, the reservoir unit V and/or themoistening unit B may be connected to the adsorption material inlet ofthe countercurrent filter apparatus 1, especially by means of apipeline.

According to the invention, more particularly, the purification plant A,in the operating state and/or use state, has and/or enables a water flowand/or stream (W), especially with a flow and/or stream of water AW tobe treated and/or purified that enters the countercurrent filterapparatus 1 and especially with a flow and/or stream of purified waterand/or filtrate Fl that exits from the countercurrent filter apparatus.More particularly, the purification plant A, in the operating stateand/or use state, should have and/or enable adsorbent transport oradsorbent flow AK, especially cyclic adsorption transport or adsorptionflow. In this connection, in accordance with the invention, moreparticularly, the water flow and/or stream W and the adsorbent transportor adsorbent flow AK in the countercurrent filter apparatus 1 run incountercurrent to one another and/or in opposite directions to oneanother.

More particularly, the purification plant of the invention may includethe countercurrent filter apparatus of the invention, as definedhereinafter.

In addition, FIG. 2 is a schematic diagram of a preferred embodiment ofthe countercurrent filter apparatus 1 according to the invention.

More particularly, FIG. 2 shows the countercurrent filter apparatus 1 ofthe invention, especially countercurrent adsorption filter column,preferably for treatment and/or purification of water, especially ofwastewater or drinking water, preferably for adsorptive removal ofinorganic- or organic-based, especially organic-based, contaminants suchas trace substances and/or micropollutants, and for uptake, storage andrelease, especially continuous uptake, storage and release, of at leastone preferably particulate adsorption material,

-   -   wherein the countercurrent filter apparatus 1 has at least one        housing 2, said housing 2 having at least one adsorption and/or        countercurrent zone 3 and at least one water entry region 4 and        at least one water exit region 5,    -   wherein the adsorption and/or countercurrent zone 3, in terms of        flow, is disposed between the water entry region 4 and the water        exit region 5 and/or wherein the adsorption and/or        countercurrent zone 3 is disposed downstream of the water entry        region 4 and upstream of the water exit region 5, based on the        flow direction of the water, and    -   wherein the water entry region 4 has at least one adsorption        material outlet 6 and wherein the water exit region 5 has at        least one adsorption material inlet 7.

More particularly, the water entry region 4 should have at least onewater feed 8 and the water exit region 5 at least one water drain 9.

Likewise, in the operating state and/or use state, in the adsorptionand/or countercurrent zone, the water to be treated and/or purified andthe adsorption material are conducted in countercurrent and/or inopposite directions to one another and/or are contacted with oneanother.

The countercurrent filter apparatus of the invention is, as shown inFIG. 1, especially designed in such a way that the adsorption and/orcountercurrent zone 3 is at least essentially tubular and/or takes theform of a tube.

In a preferred embodiment of the invention, the ratio of the height H1to the diameter D1 of the adsorption and/or countercurrent zone 3 [ratioof height H1:diameter D1] should be at least 1.5:1, especially at least2:1, preferably at least 2.5:1, more preferably at least 3:1. In thisconnection, the ratio of the height H1 to the diameter D1 of theadsorption and/or countercurrent zone 3 [ratio of height H1:diameter D1]should be in the range from 1.5:1 to 20:1, especially 2:1 to 15:1,preferably 2.5:1 to 10:1, more preferably 3:1 to 8:1.

More particularly, the countercurrent filter apparatus 1 of theadsorption and/or countercurrent zone 1 should have a height H1 of atleast 0.5 m, especially at least 0.75 m, preferably at least 1 m, morepreferably at least 2 m, especially preferably at least 3 m. Likewise,the adsorption and/or countercurrent zone 3 should have a height H1 inthe range from 0.5 m to 10 m, especially in the range from 0.75 m to 8m, preferably 1 m to 7 m, more preferably 2 m to 7 m, especiallypreferably 3 m to 5 m.

More particularly, the adsorption and/or countercurrent zone 3 of thecountercurrent filter apparatus 1 should have a diameter D1 of at most2.5 m, especially at most 2 m, preferably at most 1.5 m, more preferablyat most 1.25 m, especially preferably at most 1 m. Likewise, theadsorption and/or countercurrent zone should have a diameter D1 in therange from 0.05 to 2.5 m, especially in the range from 0.1 to 2 m,preferably 0.25 to 1.5 m, more preferably 0.5 to 1.25 m, especiallypreferably 0.5 m to 1 m.

In a preferred embodiment of the invention, the ratio of the totalheight H2 of the countercurrent filter unit 1 to the height H1 of theadsorption and/or countercurrent zone 3 [ratio of total height H2:heightH1] is at least 1.25:1, especially at least 1.5:1, preferably at least1.75:1, more preferably at least 2:1. In this connection, the ratio ofthe total height H2 of the countercurrent filter unit 1 to the height H1of the adsorption and/or countercurrent zone 3 [ratio of total heightH2:height H1] should be at most 5:1, especially at most 4.75:1,preferably at most 4.5:1, more preferably at most 4:1. In addition, theratio of the total height H2 of the countercurrent filter unit 1 to theheight H1 of the adsorption and/or countercurrent zone 3 [ratio of totalheight H2:height H1] should be in the range from 1.25:1 to 5:1,especially 1.5:1 to 4.75:1, preferably 1.75:1 to 4.5:1, preferably 2:1to 4:1.

In addition, the ratio of the diameter D1 of the adsorption and/orcountercurrent zone 3 to the diameter D2 of the water entry region 4[ratio of diameter D1:diameter D2] should be at least 1:1.1, especiallyat least 1:1.25, preferably at least 1:1.5, more preferably at least1:1.75, especially preferably at least 1:2. In this connection, theratio of the diameter D1 of the adsorption and/or countercurrent zone 3to the diameter D2 of the water entry region 4 [ratio of diameterD1:diameter D2] should be in the range from 1:1.1 to 1:5, especially1:1.25 to 1:3, preferably 1:1.5 to 1:2.5, more preferably 1:1.5 to 1:2.

More particularly, the ratio of the diameter D1 of the adsorption and/orcountercurrent zone 3 to the diameter D3 of the water exit region 5[ratio of diameter D1:diameter D3] is at least 1:1.1, especially atleast 1:1.25, preferably at least 1:1.5, more preferably at least1:1.75, especially preferably at least 1:2. In this connection, theratio of the diameter D1 of the adsorption and/or countercurrent zone 3to the diameter D3 of the water exit region 5 [ratio of diameterD1:diameter D3] is in the range from 1:1.1 to 1:5, especially 1:1.25 to1:3, preferably 1:1.5 to 1:2.5, more preferably 1:1.5 to 1:2.

According to the invention, is also advantageous in terms of flow whenthe adsorption and/or countercurrent zone 3 has an at least essentiallycircular and/or round cross section a.

In this connection, the water entry region 4 should also have an atleast essentially circular and/or round cross section b.

In the context of the present invention, it may likewise be the casethat the water exit region 5 has an at least essentially circular and/orround cross section c.

According to the invention, it is additionally preferable that thecross-sectional area a of the adsorption and/or countercurrent zone 3 isless than the cross-sectional area b of the water entry region 4 and/orless than the cross-sectional area c of the water exit region 5.

More particularly, in accordance with the invention, it may likewise bethe case that the cross-sectional area b of the water entry region 4 andthe cross-sectional area c of the water exit region 5 are at leastessentially of equal size.

In relation to the adsorption or countercurrent zone 3, in a preferredembodiment of the invention, there is thus some degree of narrowing or alower diameter or a lower cross-sectional area compared to the waterentry region 4 or the water exit region 5, which leads especially tooptimization of the flows or mass transfers or mass flows of water andadsorption material that are present in the adsorption or countercurrentzone 3, especially with regard to the avoidance or reduction of vorticesor the like or else with regard to the avoidance of what are called deadzones of reduced or zero flow, accompanied by the formation of a stablebed of the adsorption material and optimization of the contacting ofwater on the one hand and adsorption material on the other hand. Inaddition, it is also possible in this way to implement high superficialvelocities or filtering rates.

With regard to the countercurrent filter apparatus 1 of the invention,moreover, it may be the case that the adsorption and/or countercurrentzone 3, the water entry region 4 and/or the water exit region 5 arearranged such that the at least essentially circular and/or round crosssection a of the adsorption and/or countercurrent zone 3, the at leastessentially circular and/or round cross section b of the water entryregion 4 and/or the at least essentially circular and/or round crosssection c of the water exit region 5 are arranged at least essentiallyconcentrically along the longitudinal axis d of the countercurrentfilter apparatus 1.

More particularly, the countercurrent filter apparatus 1 has a firsttransition region 10. In this connection, the first transition region10, in terms of flow, should be disposed between the water entry region4 and the adsorption and/or countercurrent zone 3. Furthermore, thefirst transition region 10 should be disposed downstream of the waterentry region 4 and upstream of the adsorption and/or countercurrent zone3, based on the flow direction of the water.

Furthermore, the first transition region 10 should be frustoconicaland/or conical. In addition, the first transition region 10, proceedingfrom the water entry region 4 having the diameter D2, should narrow inthe direction of the adsorption and/or countercurrent zone 3 having thediameter D1, which likewise affords advantages in terms of flow, since afunneling function is provided to some degree for focusing the flow ofwater.

In addition, the countercurrent filter apparatus 1 should have a secondtransition region 11. In this connection, the second transition region11, in terms of flow, should be disposed between the water exit region 5and the adsorption and/or countercurrent zone 3. More particularly, thesecond transition region 11 should be disposed downstream of theadsorption and/or countercurrent zone 3 and upstream of the water exitregion 5, based on the flow direction of the water.

With regard to the second transition region 11, moreover, the lattershould be frustoconical and/or conical. In addition, the secondtransition region 10, proceeding from the water exit region 5 having thediameter D3, should narrow in the direction of the adsorption and/orcountercurrent zone 3 having the diameter D1. The second transitionregion 11 especially leads to an optimized feed of the adsorptionmaterial into the adsorption or countercurrent zone and the obtaining ofa homogeneous or optimally structured bed of the adsorption material.

The respective transition regions 10, 11 thus especially narrowproceeding from the diameter D2, D3 of the water entry region 4 or ofthe water exit region 5 to the diameter D1 of the adsorption and/orcountercurrent zone 3.

With regard, moreover, to the water feed 8 of the countercurrent filterapparatus 1 of the invention, the latter should be arranged in such away that the cross-sectional area defined by the opening of the waterfeed 8 is positioned at least essentially perpendicularly with respectto the longitudinal axis d of the countercurrent filter apparatus. Inthis way, the water can be led optimally into the apparatus.

Furthermore, it may be the case in accordance with the invention thatthe countercurrent filter apparatus 1, especially the water entry region4, has at least one distributor unit 13. In this connection, thedistributor unit 13, in terms of flow, should be disposed between thewater feed 8 of the water entry region 4 and the adsorption and/orcountercurrent zone 3 and/or between the water feed 8 of the water entryregion 4 and the first transition region 10. Likewise, the distributorunit 13 should be disposed downstream of the water feed 8 and/ordownstream of the adsorption material outlet 6, preferably downstream ofthe water feed 8 and the adsorption material outlet 6, based on the flowdirection of the water. In other words, the distributor unit 13 isespecially disposed upstream of the water feed 8 and/or the adsorptionmaterial exit 6, based on the transport direction of the adsorptionmaterial. The presence of a distributor unit 13 optimizes the entry ofthe water to be treated or purified into the adsorption orcountercurrent zone 3, which further optimizes the filter performance ofthe countercurrent filter apparatus 1 of the invention.

In this connection, the distributor unit 13 should be at leastessentially permeable and/or pervious to the water to be treated and/orpurified. Moreover, the distributor unit 13 should be at leastessentially permeable and/or pervious to the particulate adsorptionmaterial, meaning that the distributor unit 13 should have openingsand/or pores larger than the particle size of the adsorption filtermaterial, such that the spent adsorption material can get from theadsorption and/or countercurrent zone 3 to the outlet 6. For example,meshes and/or grids may be used.

In a further embodiment of the invention, the water feed 8 of the waterentry region 4 may be equipped with a cover unit. More particularly, thewater feed of the water entry region may have an assigned cover unit. Inthis connection, the cover unit, in terms of flow, should be disposedbetween the water feed of the water entry region and the adsorptionand/or countercurrent zone and/or between the water feed of the waterentry region and the first transition region. In addition, the coverunit should also be part of the distributor unit or be formed by thedistributor unit. The cover unit especially prevents ingress ofadsorption material into the water feed, especially if thecountercurrent filter apparatus is not in operation or the feed streamof water has been interrupted.

In addition, the adsorption material outlet 6 should be disposeddownstream of the water feed 8 of the water entry region 4, based on thetransport direction of the adsorption material. In other words, theadsorption material outlet 6 should be disposed upstream of the waterfeed 8 of the water entry region 4, based on the flow direction of thewater. In addition, the adsorption material outlet 6 should be disposedin an end section 12 of the water entry region 4. More particularly, theadsorption material outlet 6 should be disposed at a first end of thecountercurrent filter apparatus 1.

According to the invention, it is additionally advantageous when the endsection 12, in terms of flow, is disposed downstream of the water feed8, based on the transport direction of the adsorption material. Moreparticularly, the end section should be frustoconical and/or conical. Inthis connection, it is likewise advantageous in accordance with theinvention when the end section narrows in the direction of theadsorption material outlet 6. In this manner, a funnel or collectingfunction is provided to some degree in relation to the adsorptionmaterial to be removed.

In addition, the adsorption material outlet 6 should be disposed in sucha way that the cross-sectional area defined by the opening of theadsorption material outlet 6 is positioned at least essentiallyperpendicularly with respect to the longitudinal axis d of thecountercurrent filter apparatus 1, which improves the removal of theadsorption material.

More particularly, the adsorption material inlet 7 should be disposedupstream of the water drain 9 of the water exit region 5. In addition,the water drain 9 of the water exit region 5 should be disposeddownstream of the adsorption material inlet 7, based in each case on theflow direction of the water.

In the context of present invention, it may likewise be the case thatthe countercurrent filter apparatus 1, especially the water exit region5, has at least one separator unit 14. In this connection, it may be thecase that the separator unit 14, in terms of flow, is disposed betweenthe water drain 9 of the water exit region 5 and the adsorption and/orcountercurrent zone 3 and/or between the water drain 9 of the water exitregion 5 and the second transition region 11.

In addition, the separator unit 14 should be disposed upstream of thewater drain 9 and/or downstream of the adsorption material inlet 7,preferably upstream of the water drain 5 and downstream of the adsorbentinlet 7.

More particularly, the separator unit 14, in this connection, in termsof flow, should be disposed between the water drain 9 and the adsorptioninlet 7.

The separator unit 14 especially prevents ingress of adsorption materialinto the water drain 9 or into the filtrate to be led away.

In this connection, the separator unit 14 should be at least essentiallypermeable and/or pervious to the water to be treated and/or purified. Inaddition, the separator unit 14 should be at least essentiallyimpermeable and/or impervious to the particulate adsorption material.

It is likewise advantageous in accordance with the invention when theseparator unit 14 comprises or consists of at least one filter element.This may, for example, be a filter web or the like. More particularly,the pore size or mesh size or the size of the passage orifices of thefilter element should be less than the particle size or grain size ofthe adsorption material.

In addition, in the context of present invention, it may be the casethat the adsorption material inlet 6 is disposed such that thecross-sectional area defined by the opening of the adsorption materialinlet 6 is positioned at least essentially perpendicularly with respectto the longitudinal axis d of the countercurrent filter apparatus 1.

In a preferred embodiment of the invention, the countercurrent filterapparatus 1, especially in the operating state and/or use state, isarranged and/or aligned at least essentially vertically, based on thelongitudinal axis d of the countercurrent filter apparatus 1. In thisconnection, the water entry region 4 is thus disposed at the bottom tosome degree or forms a lower end. In this connection, the water exitregion 5 is disposed at the top, so to speak, and/or forms an upper end.

In this embodiment, it may be the case in accordance with the inventionthat, in the operating state and/or use state, the water to be treatedand/or purified flows and/or is conducted from the lower water entryregion 4 through the adsorption and/or countercurrent zone 3 to theupper water exit region 5. More particularly, in the operating stateand/or use state, the water to be treated and/or purified may flowand/or be conducted from the bottom and/or from the lower end throughthe adsorption and/or countercurrent zone 3 upward and/or to the upperend.

In addition, in this embodiment of the invention with the verticalpositioning of the countercurrent filter apparatus 1, it may be the casethat, in the operating state and/or use state, the adsorption materialis conducted from the upper water exit region 5 through the adsorptionand/or countercurrent zone 3 to the lower water entry region 4. Moreparticularly, in the operating state and/or use state, the adsorptionmaterial should be conducted from the top and/or from the upper endthrough the adsorption and/or countercurrent zone downward and/or to thelower end.

With regard, furthermore, to the adsorption material in thecountercurrent filter apparatus 1 of the invention, the adsorptionmaterial in the countercurrent filter apparatus 1, especially in theadsorption and/or countercurrent zone 3, should be in the form of a bed.The presence of the particulate adsorption material in the form of abed, especially of a loose bed, is associated with the advantage that,firstly, optimal flow of the water to be treated or purified through theadsorption material is achieved and that, secondly, the adsorptionmaterial as such can be removed from the bed or added to the bed veryefficiently.

On the basis of the specific apparatus configuration of thecountercurrent filter apparatus 1 of the invention, it is possible toachieve very high superficial velocities or filtering rates: in thisconnection, the countercurrent filter apparatus 1 may be configured suchthat, in the operating state and/or use state, a superficial velocityand/or filtering rate, calculated as the quotient of volume flow rate[m³/h] and cross-sectional area [m²], based on the adsorption and/orcountercurrent zone and based on the water to be treated and/orpurified, of at least 10 m/h, especially at least 20 m/h, preferably atleast 25 m/h, more preferably at least 30 m/h, is present and/orestablished.

More particularly, the countercurrent filter apparatus 1 is configuredsuch that, in the operating state and/or use state, a superficialvelocity and/or filtering rate, calculated as the quotient of volumeflow rate [m³/h] and cross-sectional area [m²], based on the adsorptionand/or countercurrent zone and based on the water to be treated and/orpurified, in the range from 10 m/h to 120 m/h, especially 20 m/h to 100m/h, preferably 25 m/h to 80 m/h, more preferably 30 m/h to 70 m/h,especially preferably 40 m/h to 60 m/h, is present and/or established.

It is likewise possible, on the basis of the countercurrent filterapparatus 1 of the invention, also to set optimal mass throughputs: moreparticularly, it may be the case in this connection that thecountercurrent filter apparatus 1 according to the invention isconfigured such that, in the operating state and/or use state, a massthroughput, especially a filtrate-specific mass throughput, calculatedas the quotient of mass throughput of adsorption material in thecountercurrent filter apparatus [g/h] and volume of purified waterand/or filtrate produced [m³], in the range from 10⁻⁷ g/h·m³ to 1000g/h·m³, especially 10⁻⁶ g/h·m³ to 100 g/h·m³, preferably 10⁻⁵ g/h·m³ to10 g/h·m³, is present and/or established. On the basis of thecountercurrent filter apparatus of the invention, it is thus possiblethat only small amounts of adsorption material are used for purificationof water contaminated with trace substances or microcontaminants. Thefiltrate specific mass throughput can especially also be calculated bythe general formula V_(F,m)=m_(ads,D,AP)/V_(F) (with V_(F,m):filtrate-specific mass throughput; m_(ads,D,AP) mass throughput of theadsorption material in the countercurrent filter apparatus; V_(F):volume of purified water and/or filtrate or filtrate volume produced).

Finally, FIG. 3 illustrates the principle that underlies the presentinvention of the opposite transport of water to be treated or purifiedon the one hand and of adsorption material on the other hand in thecountercurrent filter apparatus 1 of the invention, especiallycountercurrent adsorption filter column, preferably as defined above,and the contacting of water and adsorption material, especially in theadsorption and/or countercurrent zone 3 of the countercurrent filterapparatus 1 according to the invention.

FIG. 3 additionally illustrates the flow or transport of the water W onthe one hand and of the adsorption material AK on the other hand, incountercurrent to one another, that is present in the operating state oruse state in the countercurrent filter apparatus 1. This involves flowof the water W to be treated proceeding from the water entry region 4through the adsorption or countercurrent zone 3 into the water exitregion 5, while the adsorption material flows or is transportedproceeding from the water exit region 5 through the adsorption orcountercurrent zone 3, in which the adsorption material is presentpreferably in the form of a loose bed 15, into the water entry region 4.By virtue of the adsorption material being fed to the bed 15, especiallycontinuously, proceeding from the water exit region 5, and additionallybeing withdrawn from the bed 15, especially continuously, in thedirection of the water entry region 4, there is exchange, especiallycontinuous exchange, of the adsorption material in the bed 15 (moreparticularly simultaneously with the transport of the water), such thatthe bed 15 in effect is not exhausted and no operational interruptionsare required for exchange of the adsorption material.

Further configurations, adaptations, variations, modifications,peculiarities and advantages of the present invention are immediatelyapparent to and implementable by the person skilled in the art onreading the description, without leaving the realm of the presentinvention.

The present invention is illustrated by the working examples whichfollow, but these are not intended to restrict the present invention inany way.

Working Examples 1. Performance of the Method of the Invention in aPreferred Embodiment of the Present Invention:

-   -   The method of the invention, in a specific embodiment of the        present invention, can be conducted as described hereinafter:    -   The method of the invention can be conducted, for example, using        a specific adsorption material in the form of spherical        activated carbon, particularly using activated carbon in the        form of PBSAC (polymer-based spherical activated carbon).    -   The method of the invention can especially be conducted with the        aim of a preferably complete removal of trace substances from        water to be purified or treated after passing through the        countercurrent filter apparatus or adsorption stage used in        accordance with the invention, and it is also possible to        implement such a procedure, for example, in a drinking water        works for treatment or purification of drinking water. The water        to be treated or purified, which is fed to the countercurrent        filter apparatus in the context of the procedure of the        invention, can also be referred to synonymously as untreated        water, while the purified water can be referred to        correspondingly as filtrate.    -   With regard to the countercurrent filter apparatus used in the        context of the method of the invention, in this preferred        embodiment, the latter is, for example, a countercurrent filter        apparatus as defined in the corresponding apparatus claims,        which especially takes the form of a continuous countercurrent        adsorption filter column. This corresponding countercurrent        filter apparatus, in the context of the procedure of the        invention, may especially be set up or operated at least        essentially vertically, based on the longitudinal axis of the        countercurrent filter apparatus, such that there is to some        degree, and it is possible to define, an upper end and a lower        end in relation to the countercurrent filter apparatus.    -   In this case, under operating conditions or use conditions, the        (untreated) water to be treated or purified flows, especially        under pressure, into the countercurrent filter apparatus, the        water entering the countercurrent filter apparatus, to some        degree, from the bottom or at the lower end of the        countercurrent filter apparatus. In this connection, the        countercurrent filter apparatus may have a distributor which        conducts the (untreated) water to be treated or processed into        an adsorption or countercurrent zone of the countercurrent        filter apparatus.    -   At the same time, through an upper end of the countercurrent        filter apparatus or from the top, regenerated or unladen        adsorption material in the form of a specific activated carbon        is fed to the countercurrent filter apparatus, and this can        likewise be effected under pressure, in which case the pressure        for this purpose of introducing the adsorption material should        be greater than the pressure in the countercurrent filter        apparatus or in the adsorption zone. The adsorption material        subsequently passes, so to speak, into the adsorption or        countercurrent zone from the top, in which it forms a bed,        especially a loose bed, and wherein the adsorption material        falls or is transported from the top downward, especially in the        bed.    -   At the same time, the (untreated) water to be treated or        purified flows from the bottom upward in the adsorption or        countercurrent zone and hence in countercurrent to the        adsorption material, such that the removal or adsorption of the        trace substances or microcontaminants from the untreated water        can take place in countercurrent. In this way, the water is        freed of the contaminants and the adsorption material is laden        with the contaminants, and the adsorption material having the        highest loading of contaminants is correspondingly present in        the lower region of the adsorption and/or countercurrent zone.    -   The water which has been purified, i.e. freed of the trace        substances or micropollutants, can subsequently, through a        mechanical separating apparatus, enter the upper region or the        upper end and hence, as it were, the top of the countercurrent        filter apparatus, and it is possible to discharge or lead off        the purified water from this region for further use, for example        as drinking water.    -   Any separating apparatus present in the countercurrent filter        apparatus serves especially to retain the adsorption material,        and the separating apparatus for this purpose may take the form,        for example, of a filter web or wire mesh.    -   At the other end and hence, as it were, in the lower region or        at the foot of the countercurrent filter apparatus, the        adsorption material laden with the contaminants may be        withdrawn, for example using a jet pump, peristaltic pump or the        like.    -   Subsequently, the laden adsorption material can be fed to a        desorption apparatus or regeneration apparatus which may        comprise several aggregates or units.    -   In this connection, it may be the case, for example, that the        adsorption material, prior to drying, is freed of the adhering        moisture or of residual water, for example by means of an        inclined clarifier or belt drier. Subsequently, the adsorption        material can be subjected to an additional main drying        operation, in which case it is possible to use, for example,        belt driers and/or fluidized bed driers. In this way, it is        especially possible to remove residual moisture present in the        pore volume or space of the adsorption material.    -   By means of a mechanical conveying unit, for example in the form        of a vibrating channel, a pneumatic conveyor or a conveyor belt,        it is possible to feed the adsorption material thus dried and        laden with the pollutants to a thermal regeneration. For this        purpose, it is possible to use, for example, units in the form        of a rotary oven, especially an indirectly heated rotary oven, a        high-temperature fluidized bed unit or a microwave oven. In the        thermal regeneration, the contaminants are driven out of or        removed from the adsorption material with the aid of thermal        energy, such that the corresponding micropollutants are        desorbed. The desorbed substances are especially in the gaseous        state and can be sent to a thermal final utilization, especially        an incineration. The adsorption material is to some degree        returned or converted back to the original state or to an        unladen state by the thermal regeneration, and so the adsorption        capacity of the adsorption material is restored.    -   The unladen adsorption material thus recycled can be stored        intermediately, for example, in a reservoir apparatus and wetted        with water by means of a suitable moistening or conveying unit,        such as a jet pump and/or a peristaltic pump, and fed back to        the countercurrent filter apparatus, especially under pressure.    -   Because of the procedure of the invention, it is possible        overall to achieve a small circulation factor in relation to the        purifying plant used, meaning that a relatively large portion of        the adsorption material used in the context of the procedure of        the invention is in the countercurrent filter apparatus during        the procedure, and only a relatively small portion of the        adsorption material is in the regeneration step, which is        associated with advantages in terms of process technology, since        a high proportion of the adsorption material can fulfill the        process-specific purpose of the purification of water. It is        likewise possible, because of the procedure of the invention, to        achieve high specific mass throughputs, since large volumes of        filtrate can be produced in relation to the amount of adsorption        material used.

2. Studies of the Efficiency of the Purification Plant of the Inventionand of the Countercurrent Filter Apparatus of the Invention:

-   -   a1) The performance of the purification plant of the invention        and of the countercurrent filter apparatus of the invention in        relation to the purification of contaminated untreated water is        examined hereinafter in prolonged operation. The water to be        treated or purified contains, on average, the following        contaminants or trace substances:

TABLE 1 Trace substances in the water to be treated or purified(untreated water) Mean concentration at the inlet of Name thecountercurrent filter apparatus Unit Amidotrizoic acid 290 ng/lIopamidol 97 ng/l Perfluorooctane- 260 sulfonate (PFOS) Methyltert-butyl 0.57 μg/L ether (MTBE) Dissolved organic 0.4-0.7 mg/L carbons(DOC)

-   -   -   The countercurrent filter apparatus used, especially as            defined above, has a height H1 of about 3.50 m with a            diameter D2 and D3 of the water entry region and water exit            region respectively of about 1.60 m. The spatial dimensions            of the cylindrical adsorption or countercurrent zone of the            countercurrent filter apparatus are additionally 1.75 m for            the height H1 and 0.8 m for the diameter D1. The volume of            the random bed of the activated carbon used in the            countercurrent filter apparatus is about 0.85 m³.        -   The adsorption material used is a specific particulate            activated carbon (PBSAC) having a pore volume according to            Gurvich of 1.124 cm³/g and an abrasion hardness of 98.7%.        -   The superficial velocity or filtering rate is set to a value            of about 55 m/h.        -   In addition, the countercurrent filter apparatus according            to the invention or the purification plant of the invention            was run with a circulation factor, calculated as the            quotient of the amount of the adsorption material present in            the regeneration or recycling operation and the amount of            the adsorption material present in the countercurrent filter            apparatus, of about 10.        -   In addition, the countercurrent filter apparatus of the            invention is operated with a specific mass throughput,            calculated as the quotient of mass throughput of adsorption            material and volume of treated or purified water or filtrate            produced, of about 5 g/h·m³.        -   The purification plant used additionally contains a first            drying or demoistening unit in the form of an inclined            clarifier, a second drying or demoistening unit in the form            of a belt drier, and a third main drying or demoistening            unit in the form of a fluidized bed drier, arranged in            succession.        -   Connected downstream of the corresponding drying or            demoistening units is a regeneration or desorption unit in            the form of an indirectly heated rotary oven.        -   The purification plant additionally has a reservoir unit            connected downstream of the regeneration or desorption unit            and a moistening or transport unit in the form of a            water-jet pump, connected downstream in turn of the            regeneration or desorption unit.        -   The adsorbent laden with the contaminants withdrawn from the            countercurrent filter apparatus is passed through the            corresponding drying or demoistening units, with the            residual moisture content of the adsorption material thus            dried of about 0.8% by weight, based on the adsorption            material.        -   Subsequently, the adsorption material is transferred into            the regeneration or desorption unit. Thermal treatment is            effected therein, accompanied by the desorption of the            previously adsorbed contaminants.        -   The purified or regenerated or fresh adsorption material            thus obtained is stored intermediately in the reservoir            apparatus, and subsequently moistened with the moistening or            transport unit, likewise using the underlying untreated            water for this purpose, and subsequently fed back to the            countercurrent filter apparatus.        -   With regard, moreover, to the treated or purified water or            filtrate withdrawn from the countercurrent filter apparatus,            the latter was analyzed continuously during the entire            experimental or operating periods for any breakthroughs of            the underlying contaminants.        -   No breakthrough at all was found for an experimental or            operating period of 7 days; the filtrate obtained was free            of the above-cited contaminants for the entire period.

    -   a2) The experiment set out in section a1) is repeated, except        using a countercurrent filter apparatus in which the diameter D1        of the adsorption or countercurrent zone corresponds to the        respective diameters D2 and D3 of the water entry region and the        water exit region, such that the overall result is a cylindrical        countercurrent filter apparatus with no narrowing. At a        superficial velocity or filtering rate of 55 m/h, a breakthrough        is detected for amidotrizoic acid after an operating time of        about 118 h. The breakthrough time for iopamidol is about 125 h,        while a breakthrough time of 115 h is determined for PFOS. In        relation to MTBE, a breakthrough can be ascertained after 72 h.        For the DOC contaminants, the breakthrough time is about 65 h.        At a reduced superficial velocity or filtering rate of 10 m/h,        no breakthrough can be detected over the experimental and        operating period of 7 days. In addition, it is possible to        observe that the bed of the activated carbon is not entirely        homogeneous or uniform.

    -   b) In the context of a corresponding comparison, a noninventive        filter apparatus in the form of a filter system which is closed        in relation to the adsorption material is used. The comparative        filter apparatus has a height of 2 m and a diameter of 1.50 m        and contains activated carbon in the form of a random bed having        a volume of 0.85 m³, which is not exchanged over the course of        the experiment. The adsorption material used is a particulate        granular carbon. The system is operated with a superficial        velocity or filtering rate of 8 m/h, using the above-defined        untreated water contaminated with the corresponding contaminants        in this connection. In relation to amidotrizoic acid, it was        possible to identify a breakthrough after about 38 h of        operating time. The breakthrough time for iopamidol is about 40        h, while a breakthrough time of 42 h is determined for PFOS. In        relation to MTBE, a breakthrough can be ascertained after only        17 h. For the DOC contaminants, the breakthrough time is about        21 h.

    -   The studies laid out above show the excellent filter properties        of the inventive design based on the purification plant of the        invention and the countercurrent filter apparatus of the        invention, and the corresponding method of the invention,        wherein in this connection in relation to contaminated untreated        water excellent purification to obtain a pollutant-free        filtrate.

3. Studies of Adsorptive Removal of Trace Substances for VariousAdsorbents:

-   -   In addition, the breakthrough characteristics are ascertained        for relevant trace contaminants on various adsorbents in a        half-scale pilot plant.    -   To assess the adsorption characteristics of various trace        contaminants, an activated carbon filter plant composed of four        parallel filter columns is set up, the respective filter columns        (filters 1 to 4) having a diameter of 0.095 m with a        corresponding area of 0.07 m². The adsorption material to be        examined was used in a bed height of about 1.27 m in each case,        with variation in the corresponding amounts of activated carbon        between 3.2 and 5.5 kg. The adsorption material is not exchanged        over the experimental or operating period. The respective filter        columns are operated with a superficial velocity or filtering        rate of 10 m/h. The first filter column was operated with a        specifically commercially available granulated carbon, while the        second to fourth filter columns are operated with activated        carbon in the form of PBSAC, as shown in table 2; with regard to        the activated carbon PBSAC I to III, PBSAC I has the lowest        activation level and PBSAC II the highest.

TABLE 2 Product specifications of the adsorbents Filter 1 Filter 2Filter 4 Filter 3 Adsorbent conventional PBSAC PBSAC PBSAC granular I IIIII carbon BET m²/g 850 1506 1733 2084 Iodine number mg/g 850 1400 15841767 Particle size mm 0.5-2.6 about about about 0.5 0.45 0.45 Tappeddensity kg/m³ 460 535 479 355 Ash content wt. % 1.2 0.8 0.2 0.3

-   -   The feed to the pilot plant is ultrapure water, into which is        metered a mixture of various trace substances from a reservoir        vessel. For this purpose, amidotrizoic acid, iopamidol, PFOS,        DMS, MTBE and EDTA were metered in. Table 3 shows the mean feed        concentration of the trace substances:

TABLE 3 Mean feed concentration of the trace substances Mean value offeed concentration Amidotrizoic acid 290 ng/L Iopamidol 97 ng/L PFOS 260ng/L MTBE 3.9 μg/L N,N-Dimethylsulfamide 0.8 μg/L (DMS)

-   -   For the individual trace contaminants, the respective        breakthrough curves are determined, assuming a relative        concentration of 0.1 as the respective limit for the        breakthrough (i.e. quotient of effluent concentration and feed        concentration). The specific throughput (amount of water        throughput per kg of adsorbent) functions as the breakthrough        time. The following table shows the values determined in this        way:

TABLE 4 Breakthrough characteristics of the respective tracecontaminants (breakthrough at specific throughput [m³/kg]): Filter 1Filter 2 Filter 4 Filter 3 Activated carbon conventional PBSAC PBSACPBSAC granular I II III carbon Amidotrizoic acid 10 25 40 225 Iopamidol17 54 82 264 PFOS 20 38 60 >234 MTBE >5 15 37 35 DMS >5 7 8 7

-   -   Table 4 illustrates that the activated carbons based on PBSAC I        to III having the specifications cited in table 2 have        significantly better breakthrough characteristics than the        conventional granular carbon. Activated carbons of this kind are        particularly suitable for the method of the invention or for use        in the purification plant of the invention or the countercurrent        filter apparatus of the invention. Moreover, it should be stated        in relation to the present comparative study that the adsorption        material in the form of the conventional granular carbon used        which was removed after purification had ended exhibits distinct        abrasion, associated with sludge formation.    -   The present studies thus show, overall, the excellent properties        of the method of the invention and of the corresponding        purification plant and countercurrent filter apparatus of the        invention. In addition, the superiority of the adsorbents used        with preference in accordance with the invention is        demonstrated.

LIST OF REFERENCE NUMERALS

-   -   A purification plant    -   RV regeneration apparatus    -   T1 drying and/or demoistening unit    -   T2 drying and/or demoistening unit    -   T3 drying and/or demoistening unit    -   R regeneration and/or desorption unit    -   V reservoir apparatus unit    -   B moistening unit    -   AK adsorption material transport    -   W water flow and/or stream    -   AW water to be treated or purified    -   Fl purified water or filtrate    -   1 countercurrent filter apparatus    -   2 housing    -   3 adsorption and/or countercurrent zone    -   4 water entry region    -   5 water exit region    -   6 adsorption material outlet    -   7 adsorption material inlet    -   8 water feed    -   9 water drain    -   10 first transition region    -   11 second transition region    -   12 end section of the water entry region    -   13 distributor unit    -   14 separator unit    -   15 bed of the adsorption material    -   H1 height of the adsorption and/or countercurrent zone    -   D1 diameter of the adsorption and/or countercurrent zone    -   H2 total height of the countercurrent filter apparatus    -   D2 diameter of the water entry region    -   D3 diameter of the water exit region    -   a cross section or cross-sectional area of the adsorption and/or        countercurrent zone    -   b cross section or cross-sectional area of the water entry        region    -   c cross section or cross-sectional area of the water exit region    -   d longitudinal axis of the countercurrent filter apparatus

While Applicant's invention has been described in detail above withreference to specific embodiments, it will be understood thatmodifications and alterations in embodiments disclosed may be made bythose practiced in the art without departing from the spirit and scopeof the invention. All such modifications and alterations are intended tobe covered.

The present invention relates to a method for treatment and/orpurification of water, in particular wastewater or drinking water,preferably for the adsorptive removal of inorganically ororganically-based, impurities, such as trace substances and/ormicropollutants, wherein, in a counterflow filter device, e.g. acounterflow adsorption filter column, the water that is to be treatedand/or that is to be purified firstly, and, secondly, an, in particularparticulate, adsorption material are conducted in a counterflowdirection. In particular, a procedure is followed in such a manner thatthe water to be treated and/or purified is passed through a bed of theadsorption material present in the counterflow filter device for theadsorptive removal of impurities and the bed is exchanged andregenerated by preferably continuous removal and supply of theadsorption material in counterflow to the water that is to be treatedand/or that is to be purified

16-37. (canceled)
 38. A method for treatment or purification of waterfor the purpose of adsorptive removal of inorganic-based ororganic-based contaminants, wherein, in a countercurrent filterapparatus, water to be treated and purified, on the one hand, and aparticulate adsorption material, on the other hand are conducted incountercurrent to one another in such a way that the water to be treatedand purified is passed through a bed of the adsorption material presentin the countercurrent filter apparatus for adsorptive removal of thecontaminants and the bed is exchanged and regenerated by removal andsupply of the adsorption material in countercurrent to the water to betreated.
 39. The method as claimed in claim 38, wherein thecountercurrent filter apparatus is designed and provided for uptake,storage and release of the particulate adsorption material and whereinthe countercurrent filter apparatus comprises at least one housing, saidhousing comprising at least one adsorption or countercurrent zone and atleast one water entry region and at least one water exit region.
 40. Themethod as claimed in claim 38, wherein the countercurrent filterapparatus is designed and provided for uptake, storage and release ofthe particulate adsorption material and wherein the countercurrentfilter apparatus comprises at least one housing, said housing comprisingat least one adsorption or countercurrent zone and at least one waterentry region and at least one water exit region, wherein the adsorptionor countercurrent zone, in terms of flow, is disposed between the waterentry region and the water exit region, and wherein the water entryregion has at least one adsorption material outlet and wherein the waterexit region has at least one adsorption material inlet.
 41. The methodas claimed in claim 38, wherein the countercurrent filter apparatus isdesigned and provided for uptake, storage and release of the particulateadsorption material and wherein the countercurrent filter apparatuscomprises at least one housing, said housing comprising at least oneadsorption or countercurrent zone and at least one water entry regionand at least one water exit region, wherein the adsorption orcountercurrent zone, in terms of flow, is disposed between the waterentry region and the water exit region and wherein the adsorption orcountercurrent zone is disposed downstream of the water entry region andupstream of the water exit region, based on the flow direction of thewater, wherein the water entry region comprises at least one water feedand at least one adsorption material outlet and wherein the water exitregion comprises at least one water drain and least one adsorptionmaterial inlet, wherein the ratio of the diameter D1 of the adsorptionor countercurrent zone to the diameter D2 of the water entry region interms of the [ratio of diameter D1:diameter D2] is at least 1:1.1 andwherein the ratio of the diameter D1 of the adsorption or countercurrentzone to the diameter D3 of the water exit region in terms of the [ratioof diameter D1:diameter D3] is at least 1:1.1; and wherein thecountercurrent filter apparatus has a first transition region and asecond transition region, wherein the first transition region, in termsof flow, is disposed between the water entry region and the adsorptionor countercurrent zone and wherein the first transition region isdisposed downstream of the water entry region and upstream of theadsorption or countercurrent zone, based on the flow direction of thewater, wherein the first transition region is conical and, proceedingfrom the water entry region having the diameter D2, narrows in thedirection of the adsorption or countercurrent zone having the diameterD1, and wherein the second transition region, in terms of flow, isdisposed between the water exit region and the adsorption orcountercurrent zone and wherein the second transition region is disposeddownstream of the adsorption or countercurrent zone and upstream of thewater exit region, based on the flow direction of the water, wherein thesecond transition region is conical and, proceeding from the water exitregion having the diameter D3, narrows in the direction of theadsorption or countercurrent zone having the diameter D1.
 42. The methodas claimed in claim 38, wherein the adsorption material is introducedcontinuously into the countercurrent filter apparatus and wherein theadsorption material is removed continuously from the countercurrentfilter apparatus; wherein the adsorption material removed from thecountercurrent filter apparatus is sent and subjected to a continuousthermal regeneration operation with desorption of the contaminants,wherein the regenerated adsorption material is introduced continuouslyback into the countercurrent filter column; wherein water to be treatedand purified is introduced continuously into the countercurrent filterapparatus in the water entry region and wherein the treated and purifiedis removed continuously from the countercurrent filter apparatus;wherein the adsorption material is introduced continuously into thecountercurrent filter apparatus in the water exit region and wherein theadsorption material is removed continuously from the countercurrentfilter apparatus in the water exit region.
 43. The method as claimed inclaim 38, wherein water to be treated and purified, on the one hand, andthe adsorption material, on the other hand, in the countercurrent filterapparatus have at least essentially opposing flow directions and arecontacted with one another in countercurrent to one another in thecountercurrent filter apparatus.
 44. The method as claimed in claim 38,wherein water to be treated and purified which is introduced into thecountercurrent filter column is conducted through the adsorption orcountercurrent zone of the countercurrent filter apparatus disposeddownstream of the water entry region of the countercurrent filterapparatus, based on the flow direction of the water.
 45. The method asclaimed in claim 38, wherein a filtering rate, calculated as thequotient of volume flow rate [m³/h] and cross-sectional area [m²] andbased on the water to be treated and purified, of at least 10 m/h isestablished in the adsorption or countercurrent zone of thecountercurrent filter apparatus.
 46. The method as claimed in claim 38,wherein the adsorption material is fed at least essentially continuouslyto the countercurrent filter apparatus and wherein the adsorptionmaterial is conducted at least essentially continuously through thecountercurrent filter apparatus and wherein the adsorption material iswithdrawn at least essentially continuously from the countercurrentfilter apparatus; wherein the adsorption material introduced into thecountercurrent filter column is conducted through an adsorption orcountercurrent zone of the countercurrent filter apparatus disposeddownstream of the water exit region of the countercurrent filterapparatus, based on the flow direction of the adsorption material;wherein the adsorption material is present in the countercurrent filterapparatus in the form of a loose bed; and wherein the adsorptionmaterial, after passing through the adsorption or countercurrent zone ofthe countercurrent filter apparatus, is removed from the countercurrentfilter apparatus in the water entry region disposed downstream of thewater exit region of the countercurrent filter apparatus and downstreamof the adsorption or countercurrent zone of the countercurrent filterapparatus, based on the flow direction of the adsorption material. 47.The method as claimed in claim 38, wherein the adsorption material isselected from the group of particulate adsorption materials selectedfrom the group of: (i) activated carbon; (ii) zeolites; (iii) molecularsieves; (iv) metal oxide or metal particles; (v) ion exchange resins;(vi) inorganic oxides; (vii) porous organic polymers, porousorganic-inorganic hybrid polymers, metal-organic framework materials(MOFs), covalent organic frameworks materials (COFs), zeoliteimidazolate frameworks materials (ZIFs), polymer organic materials(POMs) and OFCs; (viii) mineral granulates; (ix) clathrates; and (x)mixtures or combinations thereof.
 48. The method as claimed in claim 38,wherein the adsorption material is formed from granular activatedcarbon.
 49. The method as claimed in claim 38, wherein, in the operatingstate or use state, in the adsorption or countercurrent zone, the waterto be treated or purified and the adsorption filter material areconducted in countercurrent or in opposite directions to one another.50. The method as claimed in claim 38, wherein the ratio of the heightH1 to the diameter D1 of the adsorption or countercurrent zone in termsof the [ratio of height H1:diameter D1] is at least 1.5:1 and whereinthe ratio of the height H1 to the diameter D1 of the adsorption and/orcountercurrent zone in terms of the [ratio of height H1:diameter D1] isin the range from 1.5:1 to 20:1.
 51. The method as claimed in claim 38,wherein the adsorption or countercurrent zone has an at leastessentially circular or round cross section a; wherein the water entryregion has an at least essentially circular or round cross section b;wherein the water exit region has an at least essentially circular orround cross section c; wherein the cross-sectional area a of theadsorption or countercurrent zone is less than the cross-sectional areab of the water entry region and less than the cross-sectional area c ofthe water exit region; wherein the cross-sectional area b of the waterentry region and the cross-sectional area c of the water exit region areat least essentially of equal size.
 52. The method as claimed in claim38, wherein the water entry region of countercurrent filter apparatuscomprises at least one distributor unit, wherein the distributor unit,in terms of flow, is disposed between the water feed of the water entryregion and the adsorption or countercurrent zone and between the waterfeed of the water entry region and the first transition region.
 53. Themethod as claimed in claim 38, wherein the water exit region of thecountercurrent filter apparatus comprises at least one separator unit,wherein the separator unit, in terms of flow, is disposed between thewater drain of the water exit region and the adsorption orcountercurrent zone and between the water drain of the water exit regionand the second transition region.
 54. The method as claimed in claim 38,wherein the particulate adsorption material in the adsorption orcountercurrent zone of the countercurrent filter apparatus is in theform of a loose bed.
 55. A purification plant for treatment orpurification of water for the purpose of adsorptive removal ofinorganic-based or organic-based contaminants, wherein the plantcomprises: at least one countercurrent filter apparatus, wherein, in theoperating state, the water to be treated and purified and the adsorptionmaterial are conducted in countercurrent directions to one another inthe countercurrent filter apparatus, wherein the countercurrent filterapparatus comprises at least one housing, said housing comprising atleast one adsorption or countercurrent zone and at least one water entryregion and at least one water exit region, wherein the adsorption orcountercurrent zone, in terms of flow, is disposed between the waterentry region and the water exit region and wherein the adsorption orcountercurrent zone is disposed downstream of the water entry region andupstream of the water exit region, based on the flow direction of thewater, and wherein the water entry region comprises at least oneadsorption material outlet and wherein the water exit region comprisesat least one adsorption material inlet; optionally at least one dryingor demoistening unit for drying or demoistening of adsorption materialladen with contaminants, wherein the drying or demoistening unit isdisposed downstream of the countercurrent filter apparatus, based on thetransport direction of the adsorption material; at least oneregeneration or desorption unit for regeneration of adsorption materialladen with contaminants and for provision of regenerated and unladenadsorption material, wherein the regeneration and/or desorption unit isdisposed downstream of the countercurrent filter apparatus anddownstream of the optional drying or demoistening unit, based in eachcase on the transport direction of the adsorption material; optionallyat least one moistening unit for moistening of regenerated or unladen orfresh adsorption material, wherein the moistening unit is disposeddownstream of the regeneration or desorption unit, based in each case onthe transport direction of the adsorption material.
 56. The purificationplant as claimed in claim 55, wherein the adsorption or countercurrentzone of the countercurrent filter apparatus, in terms of flow, isdisposed between the water entry region and the water exit region, andwherein the water entry region has at least one adsorption materialoutlet and wherein the water exit region has at least one adsorptionmaterial inlet.
 57. The purification plant as claimed in claim 55,wherein the countercurrent filter apparatus is designed and provided foruptake, storage and release of the particulate adsorption material andwherein the countercurrent filter apparatus comprises at least onehousing, said housing comprising at least one adsorption orcountercurrent zone and at least one water entry region and at least onewater exit region, wherein the adsorption or countercurrent zone, interms of flow, is disposed between the water entry region and the waterexit region and wherein the adsorption or countercurrent zone isdisposed downstream of the water entry region and upstream of the waterexit region, based on the flow direction of the water, wherein the waterentry region comprises at least one water feed and at least oneadsorption material outlet and wherein the water exit region comprisesat least one water drain and least one adsorption material inlet,wherein the ratio of the diameter D1 of the adsorption or countercurrentzone to the diameter D2 of the water entry region in terms of the [ratioof diameter D1:diameter D2] is at least 1:1.1 and wherein the ratio ofthe diameter D1 of the adsorption or countercurrent zone to the diameterD3 of the water exit region in terms of the [ratio of diameterD1:diameter D3] is at least 1:1.1; and wherein the countercurrent filterapparatus has a first transition region and a second transition region,wherein the first transition region, in terms of flow, is disposedbetween the water entry region and the adsorption or countercurrent zoneand wherein the first transition region is disposed downstream of thewater entry region and upstream of the adsorption or countercurrentzone, based on the flow direction of the water, wherein the firsttransition region is conical and, proceeding from the water entry regionhaving the diameter D2, narrows in the direction of the adsorption orcountercurrent zone having the diameter D1, and wherein the secondtransition region, in terms of flow, is disposed between the water exitregion and the adsorption or countercurrent zone and wherein the secondtransition region is disposed downstream of the adsorption orcountercurrent zone and upstream of the water exit region, based on theflow direction of the water, wherein the second transition region isconical and, proceeding from the water exit region having the diameterD3, narrows in the direction of the adsorption or countercurrent zonehaving the diameter D1.
 58. The purification plant as claimed in claim55, wherein the drying or demoistening unit is selected from the groupof belt driers, fluidized bed driers and inclined clarifiers andcombinations thereof; wherein the regeneration or desorption unit isselected from the group of rotary ovens, belt ovens, fluidized beddriers, and microwave ovens; wherein the moistening unit is selectedfrom the group of stirred tanks, spray towers, belt moisteners,water-jet pumps, peristaltic pumps and combinations thereof.
 59. Thepurification plant as claimed in claim 55, wherein the purificationplant also comprises at least one reservoir unit, wherein the reservoirunit is disposed downstream of the regeneration or desorption unit andupstream of the moistening unit, based on the transport direction of theadsorption material.